Flue gas adjustment

Abstract

The gas conditioning system removes pollutants, including carbon dioxide, from flue gases such as those of a ship, and includes a rotating backed bed assembly. The rotating backed bed assembly is fluidly connected to the engine's exhaust port and receives flue gas from the exhaust port. The rotating backed bed assembly includes a first rotating backed bed having an absorbent that absorbs a portion of the carbon dioxide from the flue gas, and a second rotating backed bed that receives the absorbent from the first rotating backed bed and desorbs at least a portion of the carbon dioxide from the absorbent.

Description

[Technical Field]

[0001] Cross-reference of related applications This application claims priority to U.S. Patent Application No. 63 / 508,370, filed on 15 June 2023. The disclosures of the prior application are deemed to be part of the disclosures of this application, and the entirety thereof is incorporated into this application.

[0002] This disclosure relates to gas control systems, such as those for adjusting flue gases. [Background technology]

[0003] Fuel-supplied engines, such as marine diesel engines, produce exhaust gases containing various pollutants. In marine diesel engines, these pollutants include nitrogen oxides, sulfur oxides, and carbon dioxide. U.S. and international regulations aim to limit the concentrations of certain pollutants that may be emitted by marine diesel engines. [Overview of the project]

[0004] This disclosure describes gas regulation systems, such as flue gas regulation systems for flue gases from ships.

[0005] In some embodiments, a gas conditioning system for removing contaminants, including nitrogen oxides and sulfur oxides, from a ship's flue gas includes an oxidizer having a first fluid inlet and a first fluid outlet, the oxidizer receiving exhaust flue gas from the ship's engine through the first fluid inlet at a temperature of 150°C to 550°C. The oxidizer converts at least a portion of the nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide at a temperature of 150°C to 550°C. The gas conditioning system also includes a direct contact cooler having a second fluid inlet fluid-connected to the first fluid outlet of the oxidizer, a housing defining a cooling chamber, and a second fluid outlet. The direct contact cooler cools the flue gas to a temperature of 60°C or less by bringing it into contact with seawater present in the cooling chamber. The seawater removes nitrogen dioxide and sulfur dioxide from the flue gas in the cooling chamber.

[0006] This embodiment and other embodiments may include one or more of the following features: The oxidation device can receive exhaust flue gas from a marine engine via a first fluid inlet at a temperature of 150°C to 350°C, and the oxidation device can convert at least a portion of the nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide at a temperature of 150°C to 350°C. The direct contact cooler can cool the flue gas to a temperature of 50°C or less. The oxidation device can receive exhaust flue gas from a marine engine via a first fluid inlet at a temperature of 150°C to 310°C, and the oxidation device can convert at least a portion of the nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide at a temperature of 150°C to 310°C. The oxidation device can convert at least a portion of the sulfur oxides in the flue gas to sulfur dioxide at a temperature of 150°C to 550°C, and the direct contact cooler can separate nitrogen dioxide and sulfur dioxide from the flue gas in a cooling chamber. The oxidation apparatus may include a housing defining an oxidation chamber and an oxidizing agent present in the oxidation chamber in direct contact with the exhaust flue gas. The oxidizing agent may include a solution of sodium chlorite, hydrogen peroxide, or sodium hypochlorite, which comes into contact with the flue gas and converts at least a portion of the nitrogen oxides in the flue gas into at least one of nitrogen gas or nitrogen dioxide. The oxidation apparatus may include a selective catalytic reduction unit for converting a portion of the nitrogen oxides into at least one of nitrogen gas or nitrogen dioxide at temperatures between 150°C and 550°C. The gas conditioning system may further include an adsorption unit having a third fluid inlet fluid-connected to a second fluid outlet of a direct contact cooler, the adsorption unit receiving flue gas from the direct contact cooler and removing at least a portion of residual nitrogen oxides from the flue gas of the direct contact cooler. The adsorption unit may include at least one adsorption bed, and the gas conditioning system may guide the flue gas from the third fluid inlet through at least one adsorption bed, the adsorption bed capable of reducing the nitrogen oxide content from the flue gas to less than 50 ppm. The adsorption bed can reduce the nitrogen oxide content from flue gas to less than 10 ppm. The adsorption unit can include two adsorption beds.The selective catalytic reduction unit may include a second housing defining a second chamber and a compound inlet for introducing a mist of compound solution into the second chamber, and a first fluid inlet may guide flue gas into contact with the compound solution in the second chamber. The compound solution may include urea or ammonia. The selective catalytic reduction unit may include a catalyst positioned in the second chamber, which is in contact with the flue gas and the mist of compound solution. The gas conditioning system may further include a filter positioned upstream of the first fluid inlet, which removes particulate matter and volatile hydrocarbons from the flue gas. The filter may be directly coupled to the oxidizer at the first fluid inlet of the oxidizer. The gas conditioning system may further include a blower unit positioned between the marine engine and the first fluid inlet of the oxidizer, which guides the flue gas to the oxidizer and increases the pressure of the flue gas. The gas conditioning system may further include a blower unit positioned downstream of the direct contact cooler, which generates a partial vacuum in the flow path of flue gas through the oxidizer and the direct contact cooler, thereby facilitating the flow of flue gas through the oxidizer and the direct contact cooler toward the blower unit. The direct contact cooler may include a rotating packed bed comprising a housing surrounding a cooling chamber, a rotor drum located within the housing and rotatable about a pivot axis, a seawater inlet fluid-connected to the rotor drum, a seawater outlet fluid-connected to the housing, a second fluid inlet fluid-connected to the housing, and a second fluid outlet fluid-connected to the rotor drum, wherein flue gas is guided from the second fluid inlet to the second fluid outlet, and seawater is guided from the seawater inlet to the seawater outlet. The flue gas may be positioned in counterflow with the seawater in the rotor drum when the rotating packed bed is in use. The direct contact cooler may include a seawater inlet for introducing seawater into the cooling chamber, which removes at least some of the sulfur dioxide and nitrogen dioxide from the flue gas in the cooling chamber. The gas conditioning system may further include a water treatment system that is fluidly connected to a direct contact cooler and receives seawater from the direct contact cooler, the water treatment system including a membrane and an input system for adjusting the pH of the seawater to be greater than 6.5.The gas conditioning system may further include a rotary packed bed assembly fluidly connected to a direct contact cooler, which may receive flue gas from the direct contact cooler, and the rotary packed bed assembly may include a first rotary packed bed having an absorbent that absorbs at least a portion of carbon dioxide from the flue gas, and a second rotary packed bed that receives the absorbent from the first rotary packed bed and desorbs the carbon dioxide absorbed from the absorbent. The absorbent may include a liquid solvent. The liquid solvent may include an amine solvent. The rotary packed bed assembly may include a water washing station fluidly connected to the first rotary packed bed, which washes the flue gas from the first rotary packed bed with water. The water washing station may include a filling cylinder or a rotary packed bed. The gas conditioning system may further include a storage system fluidly connected to the second rotary packed bed, which includes a compressor and a storage tank, which receives the desorbed carbon dioxide, compresses the desorbed carbon dioxide with the compressor, and stores the carbon dioxide in the storage tank.

[0007] Certain aspects of this disclosure encompass a method for adjusting flue gas from a ship. This method includes receiving exhaust flue gas from a ship's engine at a temperature of 150°C to 550°C in an oxidation chamber; converting a portion of the nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide at a temperature of 150°C to 550°C using reactants in the oxidation chamber; receiving the flue gas from the oxidation chamber in a direct contact cooler; and cooling the flue gas to a temperature of 60°C or less by bringing the flue gas into direct contact with seawater in the direct contact cooler.

[0008] These and other embodiments may include one or more of the following features: Exhaust flue gas can be received from a marine engine at a temperature of 150°C to 350°C, and a portion of the nitrogen oxides are converted at a temperature of 150°C to 350°C. Conversion using reactants within the chamber of the oxidation apparatus may further include converting a portion of the sulfur oxides in the flue gas to sulfur dioxide, and cooling the flue gas with seawater may include removing at least a portion of the sulfur dioxide and nitrogen dioxide from the flue gas with seawater in response to direct contact between the flue gas and seawater. The oxidation apparatus may include a selective catalytic reduction unit, and conversion may include converting a portion of the nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide at a temperature of 150°C to 550°C. The reactants may include a catalyst, and conversion of a portion of the nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide may include guiding the flue gas into contact with a mist of a compound solution in the chamber, and further guiding the flue gas and the mist of the compound solution toward the catalyst in the chamber. The compound solution may include a urea solution or an ammonia solution. The method may further include receiving cooled flue gas from a direct contact cooler in an adsorption unit, and removing at least a portion of residual nitrogen oxides from the cooled flue gas in the adsorption unit. Removing at least a portion of residual nitrogen oxides from the cooled flue gas may include guiding the cooled flue gas through at least one adsorption bed of the adsorption unit to reduce the nitrogen oxide content of the flue gas to less than 50 ppm, for example, less than 10 ppm. The method may further include increasing the pressure of the flue gas using a blower unit positioned between the marine engine and the oxidizer, and guiding the flue gas to the oxidizer using the blower unit. The method may further include creating a partial vacuum in the flue gas flow path through the oxidizer and the direct contact cooler using a blower unit positioned downstream of the direct contact cooler, and guiding the flue gas to flow through the oxidizer and the blower unit toward the blower unit using the blower unit.The method may further include filtering particulate matter and volatile hydrocarbons from the flue gas using a filter located upstream of the oxidation apparatus. The direct contact cooler may include a rotating packed bed, and cooling the flue gas may include directing the flue gas in the rotating packed bed into a counterflow with seawater in the rotating packed bed. Directing the flue gas in the rotating packed bed into a counterflow with seawater in the rotating packed bed may include transferring at least a portion of the sulfur dioxide and nitrogen dioxide in the flue gas to the seawater. The method may further include directing the flue gas from the direct contact cooler to a first rotating packed bed containing an absorbent, and absorbing at least a portion of the carbon dioxide from the flue gas using the absorbent in the first rotating packed bed. The method may further include directing the absorbent containing the absorbed carbon dioxide to a second rotating packed bed, and desorbing the absorbed carbon dioxide from the absorbent in the second rotating packed bed. The method may further include guiding the desorbed carbon dioxide to a storage system, compressing the carbon dioxide in a compressor in the storage system, and storing the compressed carbon dioxide in a storage tank in the storage system. The method may further include guiding the flue gas from a first rotating packed bed to a water washing station including a housing surrounding a washing chamber, and washing the flue gas with water in the washing chamber of the water washing station. Receiving exhaust flue gas from a marine engine may include receiving the exhaust flue gas at a temperature of 250°C or less, and converting some of the nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide may include converting at a flue gas temperature of 250°C or less.

[0009] Some aspects of this disclosure encompass gas conditioning systems for removing contaminants, including nitrogen oxides and sulfur oxides, from the flue gas of a ship. The gas conditioning system includes an oxidizer having a first fluid inlet and a first fluid outlet, which receives exhaust flue gas through the first fluid inlet and converts at least a portion of the nitrogen oxides in the flue gas into at least one of nitrogen gas or nitrogen dioxide, and a direct contact cooler having a rotating packed bed for bringing the flue gas into contact with seawater and cooling the flue gas to a temperature of 60°C or less. The seawater is for removing nitrogen dioxide and sulfur dioxide from the flue gas. The rotating packed bed includes a housing surrounding a cooling chamber, a rotor drum located within the housing and rotatable about a rotation axis, a seawater inlet fluid-connected to the rotor drum, a seawater outlet fluid-connected to the housing, a second fluid inlet fluid-connected to the housing and the first fluid outlet of the oxidizer, and a second fluid outlet fluid-connected to the rotor drum. Flue gas is guided from the second fluid inlet to the second fluid outlet, and seawater is guided from the seawater inlet to the seawater outlet.

[0010] This embodiment and other embodiments may include one or more of the following features: Flue gas may be positioned in opposition to seawater in a rotor drum when a rotating packed bed is in use. A seawater inlet introduces seawater into the rotor drum, and the seawater removes at least some of the sulfur dioxide and nitrogen dioxide from the flue gas in the cooling chamber. The oxidation apparatus may include a selective catalytic reduction unit, which receives exhaust flue gas at a temperature of 150°C to 350°C and converts some of the nitrogen oxides in the flue gas into nitrogen gas at a temperature of 150°C to 350°C. The selective catalytic reduction unit may include a second housing defining a second chamber and a compound inlet for introducing a mist of compound solution into the second chamber, with a first fluid inlet leading the flue gas into contact with the mist of compound solution in the second chamber. The compound solution may include urea or ammonia. The selective catalytic reduction unit may include a catalyst located in a second chamber, which comes into contact with the flue gas and a mist of the compound solution within the second chamber. The gas conditioning system may further include an adsorption unit having a third fluid inlet fluid-connected to a second fluid outlet of a direct contact cooler, the adsorption unit receiving flue gas from the direct contact cooler and removing at least a portion of residual nitrogen oxides from the flue gas of the direct contact cooler. The adsorption unit may include at least one adsorption bed, and the gas conditioning system guides the flue gas from the third fluid inlet through at least one adsorption bed, the adsorption bed reducing the nitrogen oxide content from the flue gas to less than 10 ppm. The adsorption unit may include two adsorption beds. The gas conditioning system may further include a filter located upstream of the first fluid inlet, the filter removing particulate matter and volatile hydrocarbons from the flue gas. The filter may be directly coupled to the oxidizer at the first fluid inlet of the oxidizer. The gas regulation system may further include a blower unit positioned upstream of the first fluid inlet of the oxidizer, which directs the flue gas to the oxidizer and increases the pressure of the flue gas.The gas conditioning system may further include a blower unit positioned downstream of the direct contact cooler, which generates a partial vacuum in the flow path of flue gas through the oxidizer and the direct contact cooler, thereby facilitating the flow of flue gas through the oxidizer and the direct contact cooler toward the blower unit. The gas conditioning system may further include a rotary packed bed assembly fluidly connected to the direct contact cooler to receive flue gas from the direct contact cooler, which includes a first rotary packed bed having an absorbent that absorbs at least a portion of carbon dioxide from the flue gas, and a second rotary packed bed that receives the absorbent from the first rotary packed bed and desorbs the carbon dioxide absorbed from the absorbent. The rotary packed bed assembly may include a water washing station fluidly connected to the first rotary packed bed, which washes the flue gas from the first rotary packed bed with water. The water washing station may include a filling cylinder or a rotary packed bed. The gas adjustment system is fluidly connected to a second rotating packed bed and may further include a storage system comprising a compressor and a storage tank, the storage system receiving the desorbed carbon dioxide, compressing the desorbed carbon dioxide with the compressor, and storing the carbon dioxide in the storage tank.

[0011] Certain aspects of the present disclosure encompass a method for preparing flue gas. The method includes receiving exhaust flue gas in an oxidation chamber, converting a portion of the nitrogen oxides in the flue gas into nitrogen gas or at least one of nitrogen dioxide with reactants in the oxidation chamber, and receiving the flue gas from the oxidation in a direct contact cooler, the direct contact cooler comprising a rotating packed bed, and guiding the flue gas in the rotating packed bed into contact with seawater in the rotating packed bed to cool the flue gas to a temperature of 60°C or less.

[0012] These and other embodiments may include one or more of the following features: Conversion using reactants in the chamber of the oxidation apparatus may further include converting a portion of sulfur oxides in the flue gas to sulfur dioxide; leading the flue gas in the rotating packed bed to contact seawater in the rotating packed bed may include transferring at least a portion of sulfur dioxide and nitrogen dioxide in the flue gas to seawater; leading may include leading the flue gas into a counterflow with seawater in the rotating packed bed. The oxidation apparatus may include a selective catalytic reduction unit; receiving the exhaust flue gas may include receiving the exhaust flue gas in the chamber of the selective catalytic reduction unit at a temperature of 150°C to 550°C; and converting a portion of nitrogen oxides may include converting a portion of nitrogen oxides to nitrogen gas at a temperature of 150°C to 550°C, or 150°C to 350°C. The reactants may include a catalyst, and the conversion of a portion of nitrogen oxides into nitrogen gas may include guiding the flue gas into contact with a mist of a compound solution in a chamber, and further guiding the flue gas and the mist of the compound solution toward the catalyst in the chamber. The compound solution may include a urea solution or an ammonia solution. The method may further include receiving cooled flue gas from a direct contact cooler in an adsorption unit, and removing at least a portion of residual nitrogen oxides from the cooled flue gas in the adsorption unit. Removing at least a portion of residual nitrogen oxides from the cooled flue gas may include guiding the cooled flue gas through at least one adsorption bed of the adsorption unit to reduce the nitrogen oxide content from the flue gas to less than 50 ppm or less than 10 ppm. The method may further include increasing the pressure of the flue gas in a blower unit located upstream of the oxidizer, and guiding the flue gas to the oxidizer in the blower unit. This method may further include generating a partial vacuum in the flow path of flue gas through the oxidizer and the direct contact cooler using a blower unit positioned downstream of the direct contact cooler, and guiding the flue gas through the oxidizer and the blower unit toward the blower unit using the blower unit.The method may further include filtering particulate matter and volatile hydrocarbons from the flue gas using a filter located upstream of the oxidation apparatus. The method may further include leading the flue gas from a direct contact cooler to a first rotating packed bed having an absorbent, and absorbing at least a portion of the carbon dioxide from the flue gas using the absorbent in the first rotating packed bed. The method may further include leading the absorbent containing the absorbed carbon dioxide to a second rotating packed bed, and desorbing the absorbed carbon dioxide from the absorbent in the second rotating packed bed. The method may further include leading the desorbed carbon dioxide to a storage system, compressing the carbon dioxide in a compressor in the storage system, and storing the compressed carbon dioxide in a storage tank in the storage system. The method may further include leading the flue gas from the first rotating packed bed to a water washing station having a housing surrounding a washing chamber, and washing the flue gas with water in the washing chamber of the water washing station.

[0013] In some embodiments, a gas conditioning system for removing contaminants, including nitrogen oxides and sulfur oxides, from a ship's flue gas includes a contactor, a direct contact cooler, and an adsorption unit. The contactor includes a contactor housing defining a first chamber and an oxidizer present in the first chamber, the contactor receiving exhaust flue gas from a ship's engine in the first chamber and directing the flue gas into contact with the oxidizer to convert at least some of the nitrogen oxides in the flue gas into nitrogen dioxide. The direct contact cooler includes a rotating packed bed for receiving exhaust flue gas from the contactor and directing the flue gas into contact with seawater to cool the flue gas to a temperature of 60°C or less. The seawater removes nitrogen dioxide and sulfur dioxide from the flue gas. The rotating packed bed includes a housing surrounding a cooling chamber, a rotor drum located within the housing and rotatable around a rotation axis, a seawater inlet fluid-connected to the rotor drum, a seawater outlet fluid-connected to the housing, a first fluid inlet fluid-connected to the housing, and a first fluid outlet fluid-connected to the rotor drum. Flue gas is guided from the first fluid inlet to the first fluid outlet, and seawater is guided from the seawater inlet to the seawater outlet. The adsorption unit includes a second fluid inlet fluid-connected to the first fluid outlet of the direct contact cooler and a packed cylinder. The adsorption unit receives flue gas from the direct contact cooler and removes at least some of the residual nitrogen oxides from the flue gas, reducing the nitrogen oxide content of the flue gas to less than 10 ppm.

[0014] These and other embodiments may include one or more of the following features: Flue gas may be positioned in opposition to seawater in a rotor drum when a rotating packed bed is in use. A seawater inlet may guide seawater into the rotor drum, and the seawater removes at least a portion of sulfur dioxide and nitrogen dioxide from the flue gas in a cooling chamber. The adsorption unit may include at least one adsorption bed, which guides the flue gas through at least one adsorption bed. The oxidizing agent may include a solution of sodium chlorite, hydrogen peroxide, or sodium hypochlorite. The gas conditioning system may further include a rotating packed bed assembly fluidly connected to the adsorption unit to receive flue gas from the adsorption unit, the rotating packed bed assembly including a first rotating packed bed having an absorbent that absorbs at least a portion of carbon dioxide from the flue gas, and a second rotating packed bed that receives the absorbent from the first rotating packed bed and desorbs the carbon dioxide absorbed from the absorbent. The rotary packed bed assembly may include a water washing station fluid-connected to a first rotary packed bed, which washes the flue gas from the first rotary packed bed with water. The water washing station may include a filling cylinder or a rotary packed bed. The gas conditioning system may further include a storage system fluid-connected to a second rotary packed bed, which includes a compressor and a storage tank, which receives the desorbed carbon dioxide, compresses the desorbed carbon dioxide in the compressor, and stores the carbon dioxide in the storage tank.

[0015] Certain aspects of the present disclosure encompass methods for regulating flue gas from a ship. The method includes a contactor, which includes receiving exhaust flue gas from a ship's engine into a first chamber of the contactor, which includes a contactor housing defining a first chamber and an oxidant present in the first chamber, and guiding the flue gas to contact the oxidant in the first chamber of the contactor in order to convert at least a portion of the nitrogen oxides in the flue gas into nitrogen dioxide. The method further includes a direct contact cooler, which includes receiving exhaust flue gas from the contactor in a direct contact cooler, which includes a rotating packed bed, and guiding the flue gas in the rotating packed bed to contact seawater in the rotating packed bed in order to cool the flue gas to a temperature of 60°C or less.

[0016] These and other embodiments may include one or more of the following features: The method may further include receiving cooled flue gas from a direct contact cooler in an adsorption unit, and removing residual nitrogen oxides from the flue gas in a packed cylinder of the adsorption unit. Removing residual nitrogen oxides from the flue gas may include guiding the flue gas through at least one adsorption bed of the packed cylinder to reduce the nitrogen oxide content from the flue gas to less than 10 ppm. Guiding the flue gas to contact seawater may include guiding the flue gas in a counterflow with seawater in a rotating packed bed. Guiding the flue gas in a rotating packed bed to contact seawater in the rotating packed bed may include transferring at least a portion of the sulfur dioxide and nitrogen dioxide in the flue gas to the seawater. Leading the flue gas into contact with an oxidizer in a first chamber of a contactor may include leading the flue gas into contact with a solution of sodium chlorite, hydrogen peroxide, or sodium hypochlorite present in the first chamber to convert at least some of the nitrogen oxides in the flue gas into nitrogen dioxide. The method may further include increasing the pressure of the flue gas using a blower unit positioned between the marine engine and the contactor, and leading the flue gas to the contactor using the blower unit. The method may further include filtering particulate matter and volatile hydrocarbons from the flue gas with a filter positioned upstream of the contactor. The method may further include leading the flue gas to a first rotating packed bed having an absorbent, and absorbing at least some of the carbon dioxide from the flue gas using the absorbent in the first rotating packed bed. The method may further include leading the absorbent having the absorbed carbon dioxide to a second rotating packed bed, and desorbing the absorbed carbon dioxide from the absorbent in the second rotating packed bed. This method may further include introducing the desorbed carbon dioxide into a storage system, compressing the carbon dioxide in a compressor in the storage system, and storing the compressed carbon dioxide in a storage tank in the storage system.The method may further include guiding flue gas from a first rotating packed bed to a water washing station including a housing surrounding a washing chamber, and washing the flue gas with water within the washing chamber of the water washing station.

[0017] Some aspects of this disclosure describe a gas conditioning system for removing pollutants, including carbon dioxide, from flue gas. The gas conditioning system includes a rotary packed bed assembly fluidly connected to the exhaust port of an engine, the rotary packed bed assembly receiving flue gas from the exhaust port. The rotary packed bed assembly includes a first rotary packed bed having an absorbent that absorbs a portion of the carbon dioxide from the flue gas, and a second rotary packed bed that receives the absorbent from the first rotary packed bed and desorbs at least a portion of the carbon dioxide from the absorbent.

[0018] These and other embodiments may include one or more of the following features: The absorbent may include a liquid solvent. The liquid solvent may include an amine solvent. The rotary packed bed assembly may include a water washing station fluid-connected to a first rotary packed bed, the water washing station washing flue gas from the first rotary packed bed with water. The water washing station may include a packing cylinder or a rotary packed bed. The rotary packed bed assembly may further include a third rotary packed bed in series with the first rotary packed bed, the third rotary packed bed containing a second portion of the absorbent, and the third rotary packed bed absorbing a second portion of carbon dioxide from the flue gas. The rotary packed bed assembly may further include an intercooler fluid-connected to the first and third rotary packed beds, the intercooler cooling a second portion of the absorbent and guiding the second portion of the absorbent to the first rotary packed bed. The rotary packed bed assembly may further include an intercooler fluid-coupled to a first rotary packed bed and a third rotary packed bed, the intercooler cooling a first portion of the absorbent and directing the first portion of the absorbent to the third rotary packed bed. The rotary packed bed assembly may further include a third rotary packed bed parallel to the first rotary packed bed, the first rotary packed bed receiving a first portion of flue gas, the third rotary packed bed receiving a second portion of flue gas, and the third rotary packed bed containing a second portion of the absorbent. The rotary packed bed assembly may further include a fourth rotary packed bed in series with the second rotary packed bed, the fourth rotary packed bed receiving the absorbent from the second rotary packed bed and desorbing at least a portion of the carbon dioxide from the absorbent. The rotary packed bed assembly may further include an interheater fluid-coupled to the second rotary packed bed and the fourth rotary packed bed, the interheater heating the absorbent from the second rotary packed bed and directing the absorbent to the fourth rotary packed bed. The rotary filling bed assembly may further include a fourth rotary filling bed in parallel with a second rotary filling bed, the second rotary filling bed receiving a first portion of the absorbent and the fourth rotary filling bed receiving a second portion of the absorbent.The gas adjustment system is fluidly connected to a second rotating packed bed and may further include a storage system including a compressor and a storage tank, the storage system receiving desorbed carbon dioxide, compressing the desorbed carbon dioxide with the compressor, and storing the carbon dioxide in the storage tank. The gas adjustment system may further include a selective catalytic reduction unit fluidly positioned upstream of the rotating packed bed assembly between the exhaust port and the rotating packed bed assembly, the selective catalytic reduction unit including a fluid inlet and a fluid outlet fluidly connected to the exhaust port, the selective catalytic reduction unit receiving flue gas from the exhaust port through the fluid inlet and converting at least a portion of the nitrogen oxides in the flue gas into nitrogen gas. The selective catalytic reduction unit can receive exhaust flue gas from the engine at a temperature of 150°C to 550°C and convert a portion of the nitrogen oxides in the flue gas into nitrogen gas at a temperature of 150°C to 350°C. The selective catalytic reduction unit may include a housing defining a chamber and a compound inlet for introducing a mist of compound solution into the chamber, the fluid inlet guiding the flue gas into contact with the mist of compound solution in the chamber. The compound solution may include urea or ammonia. The selective catalytic reduction unit may include a catalyst placed in a chamber, which comes into contact with the flue gas and a mist of the urea solution in the chamber. The gas conditioning system may further include an oxidation device having a fluid inlet fluidly connected to the exhaust flue gas from the engine and a fluid outlet fluidly connected to a rotating packed bed assembly, the oxidation device receiving the exhaust flue gas from the engine through the fluid inlet and converting at least a portion of the nitrogen oxides in the flue gas to nitrogen dioxide and at least a portion of the sulfur dioxide in the flue gas to sulfur dioxide. The gas conditioning system may further include a direct contact cooler fluidly positioned upstream of the rotating packed bed assembly and between the exhaust port and the rotating packed bed assembly, the direct contact cooler including a fluid inlet fluidly connected to the exhaust port, a housing surrounding a cooling chamber, and a fluid outlet, the direct contact cooler directing the flue gas into contact with seawater present in the cooling chamber and cooling the flue gas to a temperature of 60°C or less.The direct contact cooler may include a housing surrounding a cooling chamber, a rotor drum located within the housing and rotatable about a rotation axis, and a third rotating packed bed having a seawater inlet fluid-connected to the rotor drum, a seawater outlet fluid-connected to the housing, a fluid inlet fluid-connected to the housing, and a fluid outlet fluid-connected to the rotor drum, wherein flue gas is guided from the fluid inlet to the fluid outlet, and seawater is guided from the seawater inlet to the seawater outlet. The flue gas may be arranged in counterflow with the seawater in the rotor drum when the third rotating packed bed is in use. The direct contact cooler may include a seawater inlet for introducing seawater into the cooling chamber, and the seawater removes at least a portion of sulfur dioxide and nitrogen dioxide from the flue gas in the cooling chamber. The gas conditioning system may further include an adsorption unit fluidly positioned upstream of the rotating packed bed assembly and between the exhaust port and the rotating packed bed assembly, the adsorption unit having a fluid inlet fluid-connected to the exhaust port, the adsorption unit receiving flue gas from the exhaust port and removing at least a portion of nitrogen oxides from the flue gas. The adsorption unit may include at least one adsorption bed, and the gas conditioning system guides flue gas from the fluid inlet through at least one adsorption bed, which reduces the nitrogen oxide content from the flue gas to less than 10 ppm.

[0019] Specific examples of this disclosure include a method for regulating flue gas. The method includes guiding flue gas from an exhaust port to a rotating bed assembly, the rotating bed assembly comprising a first rotating bed and a second rotating bed, and absorbing at least a portion of carbon dioxide from the flue gas using an absorbent in the first rotating bed. The method also includes guiding the absorbent having absorbed carbon dioxide from the first rotating bed to the second rotating bed, and desorbing the carbon dioxide from the absorbent in the second rotating bed.

[0020] These and other embodiments may include one or more of the following features: The method may further include introducing desorbed carbon dioxide into a storage system, compressing the carbon dioxide in a compressor in the storage system, and storing the compressed carbon dioxide in a storage tank of the storage system. The method may further include introducing flue gas from a first rotating bed to a water washing station, and washing the flue gas with water in a washing chamber of the water washing station. The rotating bed assembly may further include a third rotating bed in series with the first rotating bed and containing a second portion of absorbent, and the method may further include introducing flue gas from the first rotating bed to the third rotating bed, and absorbing a second portion of carbon dioxide from the flue gas using the second portion of absorbent in the third rotating bed. The method may further include guiding a second portion of the absorbent from a third rotating packed bed to an intercooler fluid-coupled to the first and third rotating packed beds, cooling the second portion of the absorbent in the intercooler, and guiding the cooled second portion of the absorbent to the first rotating packed bed. The method may further include guiding a first portion of the absorbent from a first rotating packed bed to an intercooler fluid-coupled to the first and third rotating packed beds, cooling the first portion of the absorbent in the intercooler, and guiding the cooled first portion of the absorbent to the third rotating packed bed. The rotating packed bed assembly may further include a fourth rotating packed bed in series with the second rotating packed bed, and the method may further include guiding the absorbent from the second rotating packed bed to the fourth rotating packed bed, and desorbing at least a portion of the carbon dioxide from the absorbent in the fourth rotating packed bed. Guiding the absorbent from the second rotating packed bed to the fourth rotating packed bed may include guiding the absorbent from the second rotating packed bed to an interheater fluidly coupled to the second and fourth rotating packed beds, heating the absorbent in the interheater, and guiding the heated absorbent to the fourth rotating packed bed.The method may further include receiving flue gas from the exhaust port at a temperature of 150°C to 550°C in an oxidation chamber fluidly positioned between the exhaust port and the rotating packed bed assembly, and converting a portion of the nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide at a temperature of 150°C to 550°C using a reactant within the oxidation chamber. The reactant may include an oxidizing agent, and the conversion using the reactant within the oxidation chamber may further include converting a portion of the sulfur oxides in the flue gas to sulfur dioxide using the oxidizing agent. The oxidation apparatus may include a selective catalytic reduction unit, and the conversion may include converting a portion of the nitrogen oxides in the flue gas to nitrogen gas at a temperature of 150°C to 550°C. The reactant may include a catalyst, and the conversion of a portion of the nitrogen oxides in the flue gas to nitrogen gas may include guiding the flue gas to contact a mist of a compound solution in the chamber, and further guiding the flue gas and the mist of the compound solution toward the catalyst in the chamber. The compound solution may include a urea solution or an ammonia solution. The method may further include receiving flue gas from the exhaust port in a direct contact cooler fluidly positioned between the exhaust port and the rotating packed bed assembly, and cooling the flue gas to a temperature of 60°C or less by bringing the flue gas into direct contact with seawater within the direct contact cooler. The method may further include receiving flue gas from the direct contact cooler in an adsorption unit, and removing at least a portion of residual nitrogen oxides from the cooled flue gas in the adsorption unit. Removing at least a portion of residual nitrogen oxides from the cooled flue gas may include guiding the cooled flue gas through at least one adsorption bed of the adsorption unit to reduce the nitrogen oxide content of the flue gas to less than 50 ppm.

[0021] Details of one or more embodiments of the subject matter described herein are given in the accompanying drawings and the following description. Other features, aspects, and advantages of the subject matter will become apparent from the description, drawings, and claims. [Brief explanation of the drawing]

[0022] [Figure 1] FIG. 1 is a schematic block flow diagram of an exemplary adjustment system for conditioning flue gas from a marine engine. [Figure 2] FIG. 2 is an exemplary schematic perspective view of an exemplary rotary packed bed system that can be used in the exemplary adjustment system of FIG. 1. [Figure 3] FIG. 3 is a perspective view of an exemplary marine vessel including an exemplary gas conditioning system attached thereto. [Figure 4] FIG. 4 is a flowchart illustrating an exemplary method for conditioning flue gas from a marine vessel. [Figure 5] FIG. 5 is a flowchart illustrating another exemplary method for conditioning flue gas. [Figure 6] FIG. 6 is a flowchart illustrating another exemplary method for conditioning flue gas from a marine vessel. [Figure 7] FIG. 7 is a flowchart illustrating another exemplary method for conditioning adhesive gas. DETAILED DESCRIPTION

[0023] Like reference numerals in the various drawings indicate like elements.

[0024] The present disclosure describes a gas conditioning system for treating and conditioning flue gas, such as flue gas from a marine engine, to remove or reduce pollutant emissions from the flue gas. Pollutants include carbon dioxide (CO2), nitrogen oxides (i.e., nitrogen dioxide (NO2), nitric oxide (NO), nitrous oxide (N2O), or NO including a combination of N2O, NO2, and / or NO x )), sulfur oxides (i.e., sulfur dioxide (SO2), sulfur monoxide (SO), or SO including both SO2 and SO x), particulate matter, volatile hydrocarbons, combinations thereof, or other contaminants may be included. Vessels may include container ships, tankers, car carriers, cruise liners, or other vessels including one or more marine engines. In some examples, gas regulating systems may be retrofitted to existing vessels and positioned to receive the flue gas flow between the exhaust outlets of the marine engines and the exhaust stack outlets of the vessel.

[0025] Contaminants from the flue gas of marine diesel engines may contain higher concentrations of sulfur oxides, nitrogen oxides, or both compared to the sulfur oxide and nitrogen oxide concentrations of other land-based engine systems. The solvent used to separate contaminants from the gas flow may vary depending on the type of contaminant to be separated. In some embodiments, the gas conditioning system pre-conditions the flue gas to remove all or part of sulfur oxides, nitrogen oxides, or both before removing all or part of CO2 from the gas. For example, sulfur oxides and / or nitrogen oxides can overwhelm, degrade, or otherwise adversely affect the solvent used to remove CO2 from the flue gas, resulting in insufficient or incomplete CO2 removal. Pre-treatment of the flue gas removes or reduces sulfur oxides and / or nitrogen oxides before CO2 treatment, allowing for more efficient removal of contaminants from the flue gas while efficiently utilizing the solvent(s). In certain embodiments where the flue gas is pre-conditioned in the gas conditioning system, seawater is brought into contact with and cools the flue gas to remove NO from the flue gas. x and SO x It can be used to remove all or part of it, or both, and the seawater can be recycled and / or treated by passing it through a wastewater system (i.e., a water treatment system) before recycling.

[0026] Ships operate under U.S. and / or international emission regulations, such as those of the International Maritime Organization (IMO) 2020 under Annex VI of MARPOL. Under these emission regulations, pollutants in flue gas must be within a range of specific threshold maximums for CO2 and other pollutants. Some of these regulations have led the industry to pursue cleaner and more expensive fuels due to lower concentrations of pollutants in flue gas. However, the gas conditioning systems of this disclosure can be implemented on ships to better condition flue gas from marine engines and remove higher concentrations and more pollutants from flue gas, even when processing flue gas from engines that consume fuels with higher concentrations of sulfur.

[0027] In certain onshore flue gas treatment systems, packed beds are used to treat carbon emissions from flue gas. However, packed beds require a large footprint and may not function properly on moving platforms (e.g., not on a stationary ground-mounted platform). In gas conditioning systems of this disclosure, such as gas conditioning systems on ships, the use of large footprint devices (such as packed beds) is reduced or avoided in order to efficiently maximize limited space while maintaining sufficient operational performance. For example, a gas conditioning system may include one or more rotating packed beds (RPBs) at various stages of conditioning operations, such as direct contact cooling, CO2 absorption, CO2 release, water washing, or other operational stages typically performed by larger footprint devices such as packed beds in onshore systems. Packed beds on moving platforms, such as platforms on operating ships, may have reduced performance due to the uneven distribution of solvents caused by the moving ship. The effects of motion on the liquid / gas distribution within the bed affect bed performance for at least two reasons. The first reason is the static tilt of the bed from the vertical. The amplitude and / or period of vibration (e.g., tilt) can divert the liquid within the tower from its axial path, which is normally expected in onshore absorption or regeneration towers. The strain caused by non-verticality can lead to liquid accumulation in some parts of the tower, drying in others, and slippage of untreated gases. A second reason is the accelerating force generated by the movement of the ship's hull, which is amplified in some places by the long distance between the upper floor of the tower and the center of rotation of the tower. The radial force applied by acceleration can deviate the liquid from a uniform distribution within the tower. This uneven distribution can affect contact between the liquid and gas phases, reducing the effective area for mass transfer between the phases.The gas regulating system of this disclosure offers advantages including reduced space footprint, the ability to process various contaminants from flue gas (i.e., nitrogen oxides, sulfur oxides, CO2, and / or other contaminants), regulating operation that can be performed on a mobile platform (such as a mobile vessel), improved contaminant capture capability, improved operational flexibility (such as high turndown performance), and / or reduced energy consumption required to carry out contaminant capture from the flue gas flow.

[0028] This disclosure describes a gas regulating system for use on ships and for regulating flue gases from marine engines of ships. However, the gas regulating systems described herein may be used in other engine systems for handling other types of flue gases, such as onshore engine systems. For example, the gas regulating systems described herein may be connected to the exhaust systems of marine diesel engines on ships, or to the exhaust systems of onshore hydrocarbon combustion sources such as furnaces in manufacturing facilities, refineries, cement plants, steel mills or ironworks, mobile onshore generators, combinations thereof, or other combustion gas sources.

[0029] Figure 1 is a schematic block flow diagram of an exemplary gas conditioning system 100 for conditioning flue gas from an engine, such as a marine diesel engine of a ship. The exemplary conditioning system 100 can be implemented on a ship, but it can also be implemented on a different engine system separate from the ship. The exemplary gas conditioning system 100 receives the flue gas flow from the engine, removes pollutants from the flue gas, and releases the conditioned flue gas after the removal or reduction of pollutants. The exemplary gas conditioning system 100 includes a carbon dioxide capture system 102 for separating carbon dioxide from the flue gas flowing through the carbon dioxide capture system 102, a pre-conditioning system 200 for pre-treatment of the flue gas before it flows into the carbon dioxide system 102, and a storage system 104 for storing the carbon dioxide separated from the flue gas in the carbon dioxide system 102.

[0030] During the operation of the exemplary gas conditioning system 100, flue gas from the engine flows through the pre-conditioning system 200 to reduce or remove certain contaminants from the flue gas, such as nitrogen oxides and sulfur oxides. For example, flue gas from the engine's exhaust stack 110 is directed to the pre-conditioning system 200. In some examples, a blower 112 directs flue gas from the exhaust stack 110 (or other exhaust components of the engine) to the pre-conditioning system 200. The blower 112 increases or maintains the pressure of the flue gas to overcome any final pressure drop in the flue gas as it flows through the pre-conditioning system 200 and / or carbon dioxide capture system 102, preventing back pressure in the ship's engine. Although the blower 112 is shown in Figure 1 as being between the exhaust stack 110 and the pre-conditioning system 200, the location of the blower 112 can be changed. For example, the blower 112 can be located inside the pre-conditioning system 200 itself, such as between components or downstream after the components of the pre-conditioning system 200. In some embodiments, the blower 112 is positioned downstream of the direct contact cooler (described later) of the pre-conditioning system 200 to create a partial vacuum in the exhaust gas flow through the components of the pre-conditioning system 200 upstream of the blower 112. The partial vacuum results in a draft flow of exhaust gas toward the blower 112 through the upstream components (i.e., between the exhaust stack 110 and the blower 112). At the blower 112, the pressure of the exhaust gas is increased in preparation for flowing toward downstream components such as the carbon dioxide capture system 102. The blower 112 or additional blowers can be positioned at other locations along the exhaust gas flow to create a partial vacuum in the exhaust gas flow, increase the pressure of the exhaust gas, or both.

[0031] In the pre-conditioning system 200, once nitrogen oxides and / or sulfur oxides are removed from the flue gas, or the concentrations of nitrogen oxides and sulfur oxides have decreased to below the maximum threshold concentration in the flue gas, the resulting flue gas flows to the carbon dioxide capture system 102, where carbon dioxide is removed from the flue gas, or the concentration of carbon dioxide is reduced to below an acceptable threshold. The clean flue gas obtained from the carbon dioxide capture system 102 is released into the atmosphere, and the removed carbon dioxide is led to the storage system 104. The storage system 104, for example, receives and stores carbon dioxide while a ship is in transit.

[0032] In an exemplary gas conditioning system 100, a carbon dioxide capture system 102 receives flue gas from a pre-conditioning system 200 and removes all or part of the carbon dioxide from the flue gas. In some examples, the flue gas flow can bypass the pre-conditioning system 200 and flow directly to the carbon dioxide capture system 102 from a blower 112, engine exhaust outlet, or other engine exhaust component. The carbon dioxide capture system 102 includes a rotating packed bed assembly that is fluidly connected to the engine exhaust port and receives the flue gas. An exemplary RPB system is shown in Figure 2 and described later. The rotating packed bed assembly includes a first rotating packed bed 120 called an RPB absorber 120, which contains an absorbent for absorbing some of the carbon dioxide from the flue gas. Absorbents are substances used to capture pollutants (such as carbon dioxide) from a fluid flow (e.g., a flue gas flow) by chemisorption (amine solutions, sodium hydroxide, aqueous ammonia, carbonic anhydrase, combinations thereof, and / or other substances), physical absorption (methanol, glycol, dimethyl ether, combinations thereof, or other substances), or by a mixture of chemisorbents or physical absorbents. Absorbents can vary, for example, based on the type of pollutant that is to be absorbed or adsorbed from the flue gas. In some examples, the absorbent contains a solvent, such as a liquid solvent and / or chemical solvent, for absorbing carbon dioxide (or other pollutants). For example, the liquid solvent may include amine solvents, amino acids, sodium hydroxide (NaOH), potassium hydroxide (KOH), potassium carbonate (K2CO3), ionic liquids, inorganic solvents, combinations thereof, or other solvents. In the exemplary gas control system 100 in Figure 1, the absorbent contains an amine solvent. However, other absorbents can be used to absorb carbon dioxide and / or other pollutants from the flue gas.

[0033] The rotary packed bed assembly also includes a second rotary packed bed 122, called an RPB desorber, which receives an absorbent from the first rotary packed bed 120 and desorbs at least a portion of the carbon dioxide from the absorbent.

[0034] The RPB absorber 120 absorbs carbon dioxide from the flue gas and binds the carbon dioxide to the absorbent. For example, flue gas enters the RPB absorber 120, comes into contact with the absorbent, where CO2 enters the liquid phase and reacts with the absorbent. After absorption, the treated flue gas can exit the RPB absorber 120 and be released into the atmosphere. In some embodiments, such as the exemplary gas conditioning system 100 in Figure 1, the rotating packed bed assembly of the carbon dioxide capture system 102 also includes a water washing station 124 fluidly connected to the first rotating packed bed 120. The water washing station 124 washes the flue gas from the first rotating packed bed 120 with water, for example, to remove any residual volatile absorbent that may remain with the purified flue gas in the RPB absorber 120. The water washing station 124 can take various forms, such as a packed cylinder or a rotating packed bed, and the water in the water washing station 124 comes into contact with the flue gas from the RPB absorber 120. The captured absorbent and water can be returned to the RPB absorber 120, for example, to be recombined with the absorbent for reuse or recycling.

[0035] In some embodiments, the RPB absorber 120 may include multiple RPBs positioned in series, parallel, or in a combination of parallel and series RPBs. In an exemplary system, the RPB absorber 120 includes two series RPBs, forming a first and second RPB absorber, and the flue gas travels through the series-connected first and second RPB absorbers. The first RPB absorber may include a first portion of absorbent for absorbing a first portion of carbon dioxide in the flue gas, and the second RPB absorber may include a second portion of absorbent for absorbing a second portion of carbon dioxide in the flue gas. One or both of the first or second RPB absorbers may be fluidly connected to a water flushing station 124 for flushing the flue gas. In examples with multiple RPB absorbers, the water flushing station 124 may be connected to the last RPB absorber in the exemplary RPB assembly (e.g., the furthest downstream absorber RPB). In certain embodiments, the rotating packed bed assembly also includes an intercooler fluid-coupled between RPB absorbers. The intercooler can be used to cool an absorbent, such as a first or second portion of the absorbent, and to guide the cooled absorbent to the first or second RPB absorber. In certain examples where the RPB absorber 120 includes multiple RPBs, the intercooler can be positioned between one or more or all pairs of series RPBs. A temperature rise in the flue gas / liquid agent may occur due to higher heat absorption and lower heat capacity, which alters the equilibrium in the chamber. One or more intercoolers can control the temperature rise to approach isothermal conditions, for example. The effectiveness of mutual cooling depends at least in part on the properties of the absorbent, such as heat absorption and physical properties, as well as the ratio of gas flow rate to liquid flow rate through the RPB(s).

[0036] The number and arrangement of RPBs in the RPB absorber 120 can vary, for example, to include multiple RPBs in series, multiple RPBs in parallel, or an arrangement of RPBs including both series and parallel RPBs. For example, parallel RPBs can be used to process large amounts of flue gas at once, series RPBs can be used to better cool the absorbent, promote more complete saturation of the absorbent, capture contaminants more effectively and efficiently, reduce the amount of absorbent used, or a combination of these. The arrangement of RPBs in the RPB absorber 120 can include series RPBs, parallel RPBs, or a combination thereof to optimize the tuning of the flue gas. In some embodiments, the RPB absorber 120 may include multiple RPBs including parallel and series arrangements, and a flow controller (not shown) can guide the flue gas through one or more paths along the arrangement to optimize the characteristics of the flue gas. For example, the flow controller can direct the flue gas to two (or more) parallel RPBs when the flow of flue gas to the RPB absorber 120 increases, and / or the flow controller can direct the flue gas to two (or more) series RPBs when more complete absorption of contaminants by the absorbent is desired.

[0037] In the RPB desorber 122, the rich absorbent received from the RPB absorber 120 flows through the RPB desorber 122 and comes into contact with steam from the reboiler 126. The rich absorbent is heated to break the bonds between CO2 and the absorbent, and the CO2 is removed from the absorbent in contact with the steam. In some examples, after the CO2 has been removed from the absorbent, the absorbent can be returned to the RPB absorber 120 for reuse or recycled in another way. The CO2 captured from the RPB desorber 122 can be led to a storage system 104, which will be described later.

[0038] In some embodiments, the RPB desorber 122 may include multiple RPBs positioned in series, parallel, or in combination of parallel and series RPBs. In an exemplary system, the RPB desorber 122 includes two series RPBs, forming a first and second RPB desorber, and the absorbent moves through the series-connected first and second RPB desorbers. The first RPB desorber can remove (or desorb) a first portion of CO2 from the absorbent, and the subsequent second RPB desorber can remove a second portion of CO2 from the absorbent. In certain embodiments, the rotating bed assembly also includes an interheater fluidly coupled to the first and second RPB desorbers, such as between the RPB desorbers. The interheater can be used to heat the absorbent as it moves from the first RPB desorber to the second RPB desorber. In a particular example where the RPB detacher 122 includes multiple RPBs, the interheater can be positioned between one or more or all pairs of series RPBs.

[0039] The number and arrangement of RPBs in the RPB desorber 122 can vary, for example, to include multiple RPBs in series, multiple RPBs in parallel, or arrangements of RPBs including both series and parallel RPBs. For example, parallel RPBs can be used to process large amounts of rich absorbent at once, series RPBs can be used to increase the heating of the absorbent, promote more complete regeneration of the absorbent, desorb contaminants from the absorbent more effectively and efficiently, reduce the amount of steam required in the reboiler 126, or a combination of these. The arrangement of RPBs in the RPB desorber 122 can include series RPBs, parallel RPBs, or a combination thereof to optimize the desorption and adjustment of the absorbent. In some embodiments, the RPB desorber 122 may include multiple RPBs including parallel and series arrangements, and a flow controller (not shown) can guide the absorbent (e.g., a liquid amine solvent or other liquid solvent) through one or more paths along the arrangement to optimize the properties of the absorbent. For example, the flow controller may direct the absorbent to two (or more) parallel RPBs if the flow of absorbent to the RPB desorber 122 is increased, and / or the flow controller may direct the absorbent to two (or more) series RPBs if more complete desorption of contaminants from the absorbent is desired. In some embodiments of the RPB system incorporating one or more intercoolers and one or more interheaters, the properties of the absorbent (e.g., liquid amine solvent) and its optimal configuration can help obtain an optimal ratio between the partial pressures of water and CO2, thereby reducing the overall energy consumption during absorbent regeneration.

[0040] The carbon dioxide capture system 102 of the exemplary gas conditioning system 100 includes an RPB for initiating interaction between two fluids, such as between flue gas and absorbent in the case of RPB absorbers(s), or between absorbent and vapor in the case of RPB desorbers(s). In a particular embodiment in which the exemplary gas conditioning system 100 is deployed on a ship, the use of RPBs ensures fluid interaction and liquid distribution between the two fluids, even while the ship is moving at sea. Conversely, towers rely on gravity-driven motion for fluid interaction, and relying on gravity-driven motion on a moving platform can result in uneven liquid distribution caused by the movement of the moving platform (e.g., the movement of the ship). Instead, RPBs operate with little to no performance degradation based on uneven distribution of absorbent caused by platform movement, while reducing the overall footprint required for the fluid interaction unit compared to towers.

[0041] In some embodiments, the carbon dioxide capture system 102 of the exemplary gas conditioning system 100 may include additional components to optimize the flow rate, flow capacity, flow composition, temperature, pressure, or other properties of the flue gas, absorbent, and / or captured contaminants (e.g., carbon dioxide). For example, the carbon dioxide capture system 102 includes a first exchanger 128 positioned between the RPB absorber 120 and the RPB desorber 122, and a second exchanger 130 positioned between the RPB desorber 122 and the storage system 104. The first exchanger 128 is a heat exchanger that transfers heat between the rich absorbent (e.g., rich amine solvent) flowing from the RPB absorber 120 to the RPB desorber 122 and the lean absorbent (e.g., lean amine solvent) flowing from the RPB desorber 122 to the RPB absorber 120. In some cases, the first exchanger 128 transfers heat from the lean absorbent to the rich absorbent to lower the temperature of the lean amine solvent and raise the temperature of the rich amine solvent. The first heat exchanger 128 may include a plate and flame heat exchanger or other types of cross-exchanger. The second exchanger 130 is a cross-exchanger, gas-liquid separator, or both, which receives a mixture of water and carbon dioxide from the RPB desorber 122 and separates carbon dioxide from the water. The second exchanger 130 separates carbon dioxide from the water-CO2 mixture from the RPB desorber 122, for example, to drip water from the mixture before leading the CO2 to the storage system 104. In some cases, the second exchanger 130 includes a flash separator drum that receives a stream of water and a stream of the carbon dioxide and water mixture from the RPB desorber 122 and outputs a stream of water and a separate stream of separated carbon dioxide. The separated carbon dioxide flow into the storage system 104, and the water flow from the second exchanger 130 can be discharged or recycled in a system inside or outside the exemplary gas adjustment system 100.

[0042] The storage system 104 of the exemplary gas conditioning system 100 is fluidly connected to a downstream unit of the carbon dioxide capture system 102 (e.g., a second rotating packed bed 122) and receives the captured CO2, and optionally, water and trace impurities evaporated with the captured CO2. The storage system 104 cools the CO2 to remove water, compresses the CO2, and cools it further to liquefy the CO2 for storage. The storage system 104 includes a compressor 106, a refrigeration system 107, and a storage tank 108. The refrigeration system 107 cools the captured CO2, the compressor 106 compresses the captured CO2 to a pressure of 320 pounds / square inch absolute pressure (psia) or higher, and the storage tank 108 stores the CO2 once it reaches its liquid phase. The storage system 104 can operate to store the captured CO2 at a range of temperatures and pressures. For example, the storage system 104 operates within a temperature range of -56.6°C (-69.88°F) to 31°C (87.8°F). And / or CO2 captured within a pressure range of 5.2 bar to less than 74 bar (75.42 to 1073.28 psia) can be stored.

[0043] The pre-conditioning system 200 of the exemplary gas conditioning system 100 is positioned upstream of the carbon dioxide capture system 102 along the flue gas flow from the engine and pre-conditions the flue gas before it flows into the carbon dioxide capture system 102. The pre-conditioning system 200 conditions the flue gas to remove some or all sulfur oxides, some or all nitrogen oxides, particulate matter, volatile hydrocarbons, combinations thereof, or other contaminants from the flue gas. In some cases, removing nitrogen oxides and sulfur oxides from the flue gas before the carbon dioxide capture system 102 allows the absorbent in the carbon dioxide capture system 102 to remove CO2 from the flue gas more effectively. Otherwise, the presence of nitrogen oxides, sulfur oxides, or both in the flue gas adversely affects the performance of the absorbent and reduces the lifespan of the absorbent in the carbon dioxide capture system 102. The pre-conditioning system 200 of the exemplary gas conditioning system 100 includes a filter 202, an oxidizer 204, a direct contact cooler 206, and a polisher 208. The filter 202, the oxidizer 204, the direct contact cooler 206, and the polisher 208 are arranged in series with respect to each other so that the flue gas flows through the filter 202, then the oxidizer 204, then the direct contact cooler 206, and then the polisher 208. However, the order of these devices can be different, and one or more of these devices can be completely excluded from the pre-conditioning system 200. For example, the pre-conditioning system 200 may exclude the filter 202, the oxidizer 204, the direct contact cooler 206, the polisher 208, or any combination of these components. In a particular example, the pre-conditioning system 200 includes a flow control device (e.g., a fluid valve) and a flow path for guiding the flue gas through the pre-conditioning system 200 along a desired flow path. The flow control device and / or flow path can guide flue gas through one or more or all of the components of the pre-conditioning system 200, and can be operated so that flue gas can bypass one or more or all of the components of the pre-conditioning system 200 between the engine and the carbon dioxide capture system 102.

[0044] The filter 202 removes or reduces particulate matter, volatile hydrocarbons, or both from the flue gas. The filter 202 may include a housing having a filter medium. The filter is positioned upstream of the oxidizer 204 and the direct contact cooler 206 and filters the flue gas before it flows into the oxidizer 204 and / or the direct contact cooler 206. In some embodiments, the filter 202 may be coupled to, attached to, or integrated with the oxidizer 204, for example, by being positioned within the fluid inlet of the oxidizer 204 into which the flue gas is led.

[0045] The oxidation apparatus 204, the direct contact cooler 206, the polisher 208, or any combination thereof may include a packed bed, a packed cylinder, or any combination thereof for guiding the flue gas into contact with the material. The packed bed is a container that can be filled (partially or completely) with a material intended to contact and / or interact with a fluid flowing through the packed bed. The material can form a support structure and can be coated with a catalyst. The catalyst can be varied, such as NO x , SO x or may be selective for the reduction of other contaminants. The packed bed can have various heights and shapes. A packed cylinder is a container that is positioned within the internal space of a vessel and is (partially or completely) filled with a porous packing material. The porosity, shape, and / or positioning of the packing material provide an effective contact area between fluids, such as between a liquid phase and a vapor phase. The packing material may include one or more packing unit units positioned as a cartridge structure within the vessel to increase effective mass transfer between the fluids in contact and reduce the pressure drop of the fluid flowing through the packed cylinder. In some embodiments, the packed cylinder is smaller in size than a packed tower and can operate by a forced flow of fluid through the cylinder (i.e., as mentioned above, the packed cylinder is not gravity-driven as the packed tower operates).

[0046] The oxidation device 204 is a container or apparatus that facilitates contact between the inlet fluid and reactants to promote a chemical reaction within the inlet fluid. The reactants may include oxidizing agents such as oxygen, ozone, hydrogen peroxide, sodium hypochlorite, sodium chlorite (NaClO2), or other oxidizing agents. The oxidation device 204 may include a packed bed or packed cartridge for facilitating contact between the inlet fluid and the oxidizing agent. Contact between the inlet fluid and the oxidizing agent facilitates the conversion of one or more components of the inlet fluid into water-soluble species. In the exemplary pre-conditioning system 200 of Figure 1, the oxidation device 204 facilitates contact between the flue gas and the oxidation device to convert some or all of the NO in the flue gas into the more water-soluble NO2 species. The oxidation device 204 includes a fluid inlet and a fluid outlet, and an oxidation device housing that defines the oxidation chamber. The oxidation device 204 receives the exhaust flue gas through the fluid inlet, oxidizes all or part of the flue gas in the oxidation chamber, and guides the flue gas out through the fluid outlet. The oxidation unit 204 converts all or part of the nitric oxide (NO) present in the flue gas in the oxidation unit 204 (e.g., within the oxidation chamber) into one or both of nitrogen gas (N2) or nitrogen dioxide (NO2). In some embodiments, the oxidation unit 204 also converts all or part of the sulfur oxides (SO) present in the flue gas of the oxidation unit 204 into sulfur dioxide (SO2). N2, NO2, and SO2 are more easily separated from the flue gas than NO and SO, as will be described in more detail later.

[0047] The oxidizer 204 can support the oxidizer as a solid, liquid, or gas, and supports the oxidizer within a chamber, bringing it into contact with the flue gas flowing through the chamber. In some cases, the oxidizer is in liquid form, such as a solution of the oxidizer, and is introduced into the flue gas by cross-flow, counter-flow, or parallel flow with the flue gas. In some embodiments, the oxidizer 204 includes a contactor 220 integrated with the oxidizer 204, such as within the chamber of the oxidizer 204. The contactor 220 introduces sodium chlorite or another oxidizer into the flue gas flowing through the contactor 220. In some cases, the oxidizer is sodium chlorite, introduced into the contactor as a solution of NaClO2 in direct contact with the flue gas, such as by counter-flow or cross-flow. The contactor 220 includes a housing defining a chamber (e.g., a separate chamber of the oxidizer 204 or the same chamber), and the sodium chlorite is either present in the chamber or introduced into the chamber in liquid form via one or more nozzles or other fluid pathways. Flue gas is introduced into the chamber to come into contact with sodium chlorite. Upon contact with the flue gas, the sodium chlorite oxidizes some or all of the nitric oxide (NO) in the flue gas to nitrogen dioxide (NO2), thereby reducing the nitric oxide (NO) content. In some embodiments, a direct contact cooler 206 receives the flue gas from the contactor 220 and removes some or all of the nitrogen dioxide from the flue gas. In certain embodiments, an adsorption unit 218 (described later) receives the flue gas stream from the direct contact cooler 206 and removes some or all of any residual nitrogen oxides (NO, NO2, or both) from the flue gas before directing the flue gas stream to the carbon dioxide removal system 102.

[0048] The oxidizer 204 can receive flue gas at a range of temperatures and can still function to convert nitrogen oxides and / or sulfur oxides in the flue gas to nitrogen dioxide and / or sulfur dioxide. For example, the oxidizer 204 can receive flue gas at a low temperature of 150°C, such as 150°C, or 150°C to 550°C, 150°C to 350°C, or 150°C to 310°C, and can convert NO and / or SO present in the flue gas at that temperature (e.g., 150°C to 550°C, 350°C, or 310°C) to NO2 and / or SO2. In some embodiments, the pre-conditioning system 200 includes a heater 210 upstream of the oxidizer 204 to heat the flue gas to a desired temperature. In certain examples, the flue gas can bypass the heater and flow directly into the oxidizer 204 without being heated by the heater 210.

[0049] In some cases, the flue gas exits the engine at a temperature of approximately 250°C and can either pass through a waste heat boiler to lower the temperature of the flue gas, or pass through a heater (e.g., heater 210) or boiler to raise the temperature of the flue gas, or flow directly to a pre-conditioning system 200. In conventional combustion flue gas treatment systems, the temperature of the flue gas exiting the engine typically reaches or is heated to a temperature of approximately 350°C or higher (e.g., land-based engines) or to a temperature of approximately 350°C or higher (e.g., marine engines). Heating the flue gas to a high temperature such as 350°C or higher may make it easier to oxidize the contaminants in the flue gas to more easily remove the same contaminants. However, raising the temperature of the flue gas may require additional energy and a separate heating unit. In the exemplary gas conditioning system 100 shown in Figure 1, the oxidation unit 204 receives flue gas at a temperature below 350°C, such as 150°C to 310°C, and can oxidize selective contaminants from the flue gas without the additional energy consumption and / or heating unit that would normally be required when heating the flue gas to 310°C or above (e.g., 350°C or above).

[0050] In some embodiments, the oxidizer 204 includes a selective catalytic reduction (SCR) unit, the reactant is a catalyst, and the SCR unit uses the catalyst to convert a portion of nitrogen oxides (NO x ) to nitrogen gas (N2). The SCR unit is a container or device such as a packed bed that guides the contact between the inlet fluid and the catalyst, and the contact between the inlet fluid and the catalyst promotes the conversion of the gas and water of one or more oxide gas components of the inlet fluid to a basic version. For example, in the exemplary preconditioning system 200 of FIG. 1, the SCR unit guides the flue gas into contact with the catalyst and uses the catalyst to convert some or all of the NO in the flue gas x to nitrogen gas (N2) and water (H2O) to assist the reaction. The catalyst can be various. The SCR unit includes a chamber and a compound inlet 212 for introducing a solution of the compound into the chamber. The compound can be various. For example, the compound can include urea, ammonia, or other compounds that promote the conversion of nitrogen oxides to nitrogen gas. In some cases, the compound inlet 212 introduces the compound solution as a mist (e.g., a mist of urea, a mist of ammonia, or both), and the flue gas contacts the mist of the compound solution. The SCR unit also includes a catalyst present in the chamber to interact with the flue gas and compound mist mixture and induces a chemical reaction to convert nitrogen oxides to nitrogen gas. The following equations 1 and 2 define the chemical reactions that occur between the flue gas and the urea solution on the catalyst. 3NO + CO(NH2)2 → (5 / 2)N2 + 2H2O + CO2 Equation 1 3NO2 + 2CO(NH2)2 → (7 / 2)N2 + 4H2O + CO2 Equation 2 The following equations 3 and 4 define the chemical reactions that occur between the flue gas and the ammonia solution on the catalyst. 4NO + 4NH3 + O2 → 4N2 + 6H2O Equation 3 6NO2 + 8NH3 → 7N2 + 12H2O Equation 4 Nitrogen gas is not considered a pollutant and is virtually inert in flue gas. Nitrogen oxides (NO xConverting contaminants into nitrogen gas, water, and carbon dioxide effectively reduces the concentration of nitrogen-based contaminants in flue gas or eliminates their presence. Catalysts can vary. In some embodiments, the catalyst includes a porous medium, such as a honeycomb structure of material, arranged in a chamber to interact with the flue gas and compound solution mixture. However, catalysts can take other forms, shapes, and materials. For example, the catalyst may include a packed bed of porous medium, and the catalyst material may include coated aluminum, ceramic material, or other material. In some cases, the porous medium provides a desired pressure drop for the fluid flowing through the catalyst.

[0051] A direct contact cooler 206 is a container or device that cools an inlet fluid by guiding the inlet fluid into direct contact with a cooler fluid. The direct contact cooler 206 may include a packed bed or packed cartridge to guide the contact between the inlet fluid and the cooler fluid. The contact between the inlet fluid and the cooler fluid may be counterflow, parallel flow, crossflow, or another relative flow direction. The direct contact cooler 206 of an exemplary gas conditioning system 100 includes a fluid inlet, a fluid outlet, and a cooling chamber defined by the housing of the direct contact cooler 206. The fluid inlet may be directly connected to the fluid outlet of the oxidizer 204, to the filter 202, to the blower 112, or to the exhaust components of the engine to receive the flue gas flow. The direct contact cooler 206 guides the flue gas into contact with seawater present in the cooling chamber, such as seawater entering through the seawater inlet 214, and cools the flue gas to a desired temperature with the seawater. The desired temperature can vary, such as 60°C or below, or 50°C or below, for example, 40°C.

[0052] Onboard a vessel, the direct contact cooler 206 has access to abundant seawater, and the temperature of the seawater (e.g., below 32°C) is lower than the temperature of the flue gas entering the direct contact cooler 206. When the seawater comes into contact with the flue gas, it cools the flue gas to a lower temperature, such as 60°C, 50°C, 40°C, or another temperature lower than 60°C or 50°C. In addition to cooling the flue gas, the seawater can remove nitrogen dioxide, sulfur dioxide, or both nitrogen dioxide and sulfur dioxide from the flue gas in the cooling chamber. The seawater has a basic pH (e.g., pH 8.0–8.2), and in some cases, the solubility of NO2 and / or SO2 in water allows the seawater to remove SO2 and / or NO2 from the flue gas without other catalysts or solvents.

[0053] Removing NO2 and / or SO2 from flue gases with seawater can lower the pH of the seawater. In some embodiments, the pre-conditioning system 200 includes a water treatment system 216 that receives seawater for use in the direct contact cooler 206 and treats the seawater to adjust its pH, turbidity, polycyclic aromatic hydrocarbon (PAH) content, and / or nitrate content. The water treatment system 216 treats the seawater to enable discharge of used seawater overboard, but still complies with regulatory requirements for seawater disposal or recycling. The water treatment system 216 of an exemplary gas conditioning system 100 includes a housing defining an internal chamber, a membrane (e.g., a ceramic membrane) positioned within the internal chamber, and an injection system (using NaOH or another buffer solution) for adjusting the pH of the seawater to be above an acceptable limit for overboard disposal (e.g., pH above 6.5). During operation, seawater is introduced into the internal chamber and comes into contact with the membrane, and the injection system supplies the conditioning solution to the internal chamber. The injection system may include a dosing pump for supplying a controlled amount of the conditioning solution to the outflow seawater. The water treatment system 216 may also include temperature sensors for monitoring the seawater temperature to ensure that the seawater temperature is maintained below a maximum threshold temperature, such as 60°C as established by IMO 2020.

[0054] In some embodiments, the direct contact cooler 206 includes a rotating packed bed (RPB) that guides the flue gas into contact with seawater. Figure 2 is a schematic perspective view of an exemplary rotating packed bed system 250 that can be used in the exemplary gas conditioning system 100 of Figure 1, including a direct contact cooler 206 for guiding the flue gas into a counterflow with seawater. The exemplary RPB system 250 includes a housing 252 surrounding a chamber 254 and a rotor drum 256 located within the housing 252 and rotatable about a rotation axis AA. In some embodiments, the exemplary RPB system 250 includes a motor 258 connected to the rotor drum 256 by a drive shaft or the like (e.g., directly or indirectly coupled) to drive the rotation of the rotor drum 256 about the rotation axis AA. The rotor drum 256 defines a radial flow path through the body of the rotor drum 256 between the radial outer surface of the rotor drum 256 and the interior of the rotor drum 256. In some cases, the radial flow path includes a separate radial channel through the body of the rotor drum, extending from an opening on the outer surface of the rotor drum to the internal space of the rotor drum close to its radial center (i.e., near the axis of rotation AA). The radial flow path can define an array of paths that fluidly connect the open space in the chamber 254 to the interior of the rotor drum 256. In certain embodiments, the rotor drum 256 may contain a filler material, which can define radial flow paths through the rotor drum 256. The filler material can facilitate contact and mass transfer between the liquid and gas flowing through the exemplary RPB system 250.

[0055] An exemplary RPB system 250 includes a fluid inlet 260 fluid-connected to the interior of the rotor drum 256, a fluid outlet 262 fluid-connected to the chamber 254 on the inner surface of the housing 252, a gas inlet 264 fluid-connected to the chamber 254 on the inner surface of the housing 252, and a gas outlet 266 fluid-connected to the interior of the rotor drum 256. During operation of the RPB system 250, liquid flows into the interior of the rotor drum 256 through the liquid inlet 260, and the rotation of the rotor drum 256 directs the liquid flow through the radial passage of the rotor drum 256 radially outward relative to the axis of rotation AA. As the liquid flows out from the outer surface of the rotor drum 256, the liquid subsequently flows toward the liquid outlet 262 on the inner wall of the housing 252. Conversely, gas flows into the chamber 254 through the gas inlet 264, flows toward the interior of the rotor drum 256 into the radial passage of the rotor drum 256, and subsequently flows toward the gas outlet 266. In the exemplary RPB system 250 shown in Figure 2, the gas and liquid are arranged in a counterflow manner within the radial flow path of the rotor drum 256, such that the liquid flow is in the opposite direction to the gas flow. For example, the liquid flows radially outward through the rotor drum 256 relative to the rotation axis AA, and the gas flows radially inward through the rotor drum 256 relative to the rotation axis AA, and the gas and liquid come into contact in a counterflow manner so that they flow opposite to each other. In some embodiments, the liquid flows radially outward through the rotor drum in response to the centrifugal force from the rotation of the rotor drum 256, which provides a high surface area for mass transfer between the gas and liquid as the counterflow gas comes into contact with the droplet toward the outer radial surface of the rotor drum 256.

[0056] In the exemplary RPB system 250 shown in Figure 2, the rotor drum 256 is oriented so that its axis of rotation AA is horizontal. However, this configuration and orientation can vary. For example, the rotor drum 256 can be oriented to rotate around an axis that is horizontal, vertical, or an intermediate angle between vertical and horizontal.

[0057] Referring again to the direct contact cooler 206 of the exemplary gas conditioning system 100 in Figure 1, the direct contact cooler 206 may include an RPB, as in the exemplary RPB system 250 in Figure 2. For example, the direct contact cooler 206 may include a housing surrounding a cooling chamber, a rotor drum located within the housing and rotatable about a rotation axis, a seawater inlet fluid-connected to the rotor drum, a seawater outlet fluid-connected to the housing, a second fluid inlet fluid-connected to the housing, and a second fluid outlet fluid-connected to the rotor drum. In exemplary operation, flue gas is guided from the second fluid inlet to the second fluid outlet, and seawater is guided from the seawater inlet to the seawater outlet, and when a rotating packed bed is used (e.g., the rotor drum is rotating), the flue gas is positioned in counterflow with the seawater in the rotor drum. During operation, seawater is guided into the cooling chamber, and the seawater can remove at least a portion of sulfur dioxide, nitrogen dioxide, or both from the flue gas in the cooling chamber. In some cases, the flue gas can be positioned in parallel with the seawater.

[0058] Polisher 208 is a container or device that removes trace amounts of contaminants from a fluid by reaction or adsorption using a porous medium. Polisher 208 may include a filled bed or filled cartridge to guide contact between the fluid and the material. For example, in the exemplary pre-conditioning system 200 of Figure 1, Polisher 208 removes SO4 from the flue gas before the flue gas enters the carbon dioxide capture system 102. x and / or NO xTo remove residual traces, the flue gas is guided to come into contact with particles on the support structure within the cylinder of the polisher 208. The polisher 208 in an exemplary pre-conditioning system 200 includes an adsorption unit 218 containing a filling cylinder, a fluid inlet fluid-connected to the fluid outlet of a direct contact cooler 206, and a fluid outlet. The adsorption unit 218 receives flue gas from the direct contact cooler 206 and removes all or part of the residual nitrogen oxides (e.g., NO, NO2, or both) from the flue gas. In some embodiments, the flue gas flow bypasses the polisher 208, or the polisher 208 is completely removed, for example, when the flue gas has a nitric oxide (NO) concentration below a maximum threshold concentration. For example, if the oxidizer 204 converts all (completely or substantially) of the nitric oxide (NO) in the flue gas to nitrogen dioxide (NO2), and then the direct contact cooler 206 removes nitrogen dioxide from the flue gas, the polisher 208 can be bypassed or excluded from the pre-conditioning system 200. However, if the oxidizer 204 converts only a portion of the NO to NO2, and the concentration of NO in the flue gas after the oxidizer 204 and the direct contact cooler 206 exceeds the maximum threshold concentration, the flue gas flow is directed to the polisher 208, and the adsorption unit 218 can remove some or all of the residual NO from the flue gas before it flows to the carbon dioxide removal system 102. x In certain cases, such as when an SCR unit is included that provides residual NO (which remains in the flue gas), the polisher 208 is used to remove residual NO from the flue gas. x Some or all of it can be removed. However, the SCR unit converts nitrogen oxides in the flue gas into nitrogen gas, and NO in the flue gas. x If the remaining amount is zero or otherwise below the maximum threshold concentration, the flue gas can bypass the polisher 208, or the polisher 208 can be completely excluded from the pre-conditioning system 200.

[0059] The adsorption unit 218 can take various forms. In some cases, the adsorption unit includes one or more adsorption beds (e.g., one, two, or more adsorption beds), and the flue gas is guided through one or more of the adsorption beds. Each adsorption bed can reduce the nitrogen oxide content from the flue gas to below a threshold nitrogen concentration, such as 50 ppm or less, 10 ppm or less, or another concentration less than 50 ppm. In examples where the adsorption unit includes two or more adsorption beds, one adsorption bed is used at a time, the first adsorption bed is saturated with flue gas, and the other adsorption beds are regenerated, for example, by applying heat and a sweeping airflow to the other adsorption beds.

[0060] Some components or all of the exemplary gas conditioning system 100 can be housed in a single housing, such as in a vessel or housing type, for modular positioning of the gas conditioning system 100. The housing can be mounted on a ship, located in a factory, or positioned in close proximity to an engine's exhaust system and fluidly connected to the exhaust system, in order to handle the gas flowing through the exemplary gas conditioning system 100. For example, Figure 3 is a perspective view of an exemplary ship 300 including a gas conditioning system 302 mounted on the deck of the exemplary ship 300. The exemplary ship 300 includes a ship's engine (not shown) and an exhaust system 304, and the gas conditioning system 302 is connected to the exhaust system 304, takes in flue gas through the exhaust system 304, and conditions the flue gas to remove, for example, contaminants. The gas conditioning system 302 may be the same as the exemplary gas conditioning system 100 in Figure 1, but may be mounted in a vessel and on the exemplary ship 300.

[0061] Figure 3 shows an exemplary gas regulation system 302 installed on a ship, but the gas regulation system 302 can be used in different exhaust systems and / or other technological spaces other than ships.

[0062] Figure 4 is a flowchart illustrating an exemplary method 400 for adjusting flue gas. The exemplary method 400 can be performed by the exemplary gas adjustment system 100 in Figure 1 and can be used to adjust flue gas from a vessel such as the exemplary vessel 300 in Figure 3. In 402, exhaust flue gas from a marine engine is received in an oxidation chamber at a temperature of 150°C to 350°C. In 404, some of the nitrogen oxides in the flue gas are converted to nitrogen gas or nitrogen dioxide at a temperature of 150°C to 350°C using reactants in the oxidation chamber. In 406, the flue gas from the oxidation chamber is received in a direct contact cooler. In 408, the flue gas is cooled to a temperature of 50°C or less by direct contact between the flue gas and seawater in the direct contact cooler.

[0063] Figure 5 is a flowchart illustrating another exemplary method 500 for adjusting flue gas. The exemplary method 500 can be performed by the exemplary gas adjustment system 100 of Figure 1 and can be used to adjust flue gas from a vessel such as the exemplary vessel 300 of Figure 3. In 502, exhaust flue gas is received in the chamber of an oxidizer. In 504, some of the nitrogen oxides in the flue gas are converted to nitrogen gas or nitrogen dioxide using reactants in the chamber of the oxidizer. In 506, the flue gas from the oxidizer is received in a direct contact cooler. The direct contact cooler comprises a rotating packed bed. In 508, the flue gas in the rotating packed bed is directed in a counterflow with seawater in the rotating packed bed to cool the flue gas to a temperature of 50°C or less.

[0064] Figure 6 is a flowchart illustrating another exemplary method 600 for regulating flue gas from a ship. Exemplary method 600 can be performed by the exemplary gas regulating system 100 of Figure 1 and can be used to regulate flue gas from a ship such as the exemplary ship 300 of Figure 3. In 602, exhaust flue gas from a ship's engine is received in a first chamber of a contactor. The contactor comprises a contactor housing defining the first chamber and an oxidizer present in the first chamber. In 604, the flue gas is guided to contact the oxidizer in the first chamber of the contactor to convert at least some of the nitrogen oxides in the flue gas into nitrogen dioxide. In 606, the exhaust flue gas from the contactor is received in a direct contact cooler. The direct contact cooler comprises a rotating packed bed. In 608, the flue gas in the rotating packed bed is guided to contact seawater in the rotating packed bed to cool the flue gas to a temperature of 50°C or less.

[0065] Figure 7 is a flowchart illustrating another exemplary method 700 for adjusting adhesive gas. The exemplary method 700 can be performed by the exemplary gas adjustment system 100 of Figure 1 and can be used to adjust flue gas from a vessel such as the exemplary vessel 300 of Figure 3. In 702, flue gas is led from the exhaust port to a rotating packed bed assembly. The rotating packed bed assembly comprises a first rotating packed bed and a second rotating packed bed. In 704, at least a portion of the carbon dioxide is absorbed from the flue gas by an absorbent. In 706, the absorbent with the absorbed carbon dioxide is led from the first rotating packed bed to the second rotating packed bed. In 708, the carbon dioxide is desorbed from the absorbent in the second rotating packed bed.

[0066] In a first embodiment, a gas conditioning system for removing pollutants, including carbon dioxide, from flue gas comprises a rotary packed bed assembly fluidly connected to the exhaust port of an engine, the rotary packed bed assembly configured to receive flue gas from the exhaust port, the rotary packed bed assembly comprising a first rotary packed bed containing an absorbent configured to absorb a portion of the carbon dioxide from the flue gas, and a second rotary packed bed configured to receive the absorbent from the first rotary packed bed and to desorb at least a portion of the carbon dioxide from the absorbent.

[0067] In the second embodiment according to the first embodiment, the absorbent contains a liquid solvent.

[0068] In the third embodiment according to the second embodiment, the liquid solvent includes an amine solvent.

[0069] In a fourth embodiment according to any of the aforementioned embodiments, the rotary bed assembly further comprises a water washing station fluidly connected to a first rotary bed, the water washing station being configured to wash flue gas from the first rotary bed with water.

[0070] In the fifth embodiment according to the fourth embodiment, a water washing station, a filling cylinder, or a rotating filling bed is provided.

[0071] In a sixth embodiment according to any of the aforementioned embodiments, the rotary bed assembly further comprises a third rotary bed in series with the first rotary bed, the third rotary bed comprising a second portion of an absorbent, and configured to absorb a second portion of carbon dioxide from the flue gas.

[0072] In a seventh aspect according to the sixth aspect, the rotary bed assembly further comprises an intercooler fluid-coupled to a first rotary bed and a third rotary bed, the intercooler configured to cool a second portion of the absorbent and guide the second portion of the absorbent to the first rotary bed.

[0073] In the eighth aspect according to the sixth aspect, the rotary bed assembly further comprises an intercooler fluid-coupled to a first rotary bed and a third rotary bed, the intercooler configured to cool a first portion of the absorbent and guide the first portion of the absorbent to the third rotary bed.

[0074] In a ninth aspect according to any of the aforementioned embodiments, the rotary bed assembly further comprises a third rotary bed parallel to a first rotary bed, the first rotary bed being configured to receive a first portion of flue gas, the third rotary bed being configured to receive a second portion of flue gas, and the third rotary bed containing a second portion of absorbent.

[0075] In a tenth embodiment according to any of the aforementioned embodiments, the rotary bed assembly further comprises a fourth rotary bed in series with a second rotary bed, the fourth rotary bed being configured to receive an absorbent from the second rotary bed and to desorb at least a portion of the carbon dioxide from the absorbent.

[0076] In the eleventh aspect according to the tenth aspect, the rotary bed assembly further comprises an interheater fluid-coupled to a second rotary bed and a fourth rotary bed, the interheater being configured to heat the absorbent in the second rotary bed and guide the absorbent to the fourth rotary bed.

[0077] In a twelfth aspect according to any of the aforementioned embodiments, the rotary bed assembly further comprises a fourth rotary bed parallel to a second rotary bed, the second rotary bed being configured to receive a first portion of the absorbent, and the fourth rotary bed being configured to receive a second portion of the absorbent.

[0078] In a thirteenth embodiment according to any of the aforementioned embodiments, the gas conditioning system further comprises a storage system fluidly connected to a second rotating packed bed, the storage system comprising a compressor and a storage tank, the storage system being configured to receive desorbed carbon dioxide, compress the desorbed carbon dioxide with the compressor, and store the carbon dioxide in the storage tank.

[0079] In a 14th embodiment according to any of the above-described embodiments, the gas conditioning system further comprises a selective catalytic reduction unit fluidly positioned upstream of the rotating bed assembly between an exhaust port and the rotating bed assembly, the selective catalytic reduction unit comprising a fluid inlet and a fluid outlet fluidly connected to the exhaust port, the selective catalytic reduction unit being configured to receive flue gas from the exhaust port through the fluid inlet and to convert at least a portion of the nitrogen oxides in the flue gas into nitrogen gas.

[0080] In the 15th aspect according to the 14th aspect, the selective catalytic reduction unit receives exhaust flue gas from the engine at a temperature of 150°C to 550°C and converts a portion of the nitrogen oxides in the flue gas into nitrogen gas at a temperature of 150°C to 550°C.

[0081] In the 16th aspect according to the 15th aspect, the selective catalytic reduction unit receives exhaust flue gas from the engine at a temperature of 150°C to 350°C and converts a portion of the nitrogen oxides in the flue gas into nitrogen gas at a temperature of 150°C to 350°C.

[0082] In the 17th aspect according to the 16th aspect, the selective catalytic reduction unit receives exhaust flue gas from the engine at a temperature of 150°C to 310°C and converts a portion of the nitrogen oxides in the flue gas into nitrogen gas at a temperature of 150°C to 310°C.

[0083] In an 18th embodiment, which is one of the 14th to 17th embodiments, the selective catalytic reduction unit comprises a housing defining a chamber and a compound inlet configured to introduce a mist of compound solution into the chamber, the fluid inlet configured to guide a flue gas into contact with the mist of compound solution in the chamber.

[0084] In the 19th aspect according to the 18th aspect, the compound solution contains urea or ammonia.

[0085] In the 20th embodiment according to the 18th or 19th embodiment, the selective catalytic reduction unit includes a catalyst placed in a chamber, the catalyst being configured to come into contact with flue gas and a mist of compound solution in the chamber.

[0086] In a 21st embodiment, which is one of the first to 13 embodiments, the gas conditioning system further comprises an oxidation device having a fluid inlet fluidly connected to exhaust flue gas from an engine and a fluid outlet fluidly connected to a rotating packed bed assembly, the oxidation device being configured to receive exhaust flue gas from the engine through the fluid inlet and to convert at least a portion of the nitrogen oxides in the flue gas to nitrogen dioxide and at least a portion of the sulfur oxides in the flue gas to sulfur dioxide.

[0087] In a 22nd embodiment according to any of the above-described embodiments, the gas conditioning system further comprises a direct contact cooler positioned upstream of the rotary bed assembly and fluidly positioned between the exhaust port and the rotary bed assembly, the direct contact cooler comprising a fluid inlet fluidly connected to the exhaust port, a housing surrounding a cooling chamber, and a fluid outlet, the direct contact cooler being configured to guide flue gas into contact with seawater present in the cooling chamber and to cool the flue gas to a temperature of 60°C or less.

[0088] In the 23rd aspect according to the 22nd aspect, the direct contact cooler is configured to guide the flue gas into contact with seawater present in the cooling chamber, thereby cooling the flue gas to a temperature of 50°C or less.

[0089] In the 24th embodiment according to the 22nd or 23rd embodiment, the direct contact cooler comprises a housing surrounding a cooling chamber, a rotor drum located within the housing and rotatable about a pivot axis, and a third rotating packed bed having a seawater inlet fluid-connected to the rotor drum, a seawater outlet fluid-connected to the housing, a fluid inlet fluid-connected to the housing, and a fluid outlet fluid-connected to the rotor drum, wherein flue gas is guided from the fluid inlet to the fluid outlet, and seawater is guided from the seawater inlet to the seawater outlet.

[0090] In the 25th aspect according to the 24th aspect, the flue gas is positioned in opposition to the seawater in the rotor drum when the third rotating packed bed is in use.

[0091] In a 26th embodiment, which is one of the 22nd to 25th embodiments, the direct contact cooler is provided with a seawater inlet for introducing seawater into a cooling chamber, and the seawater is configured to remove at least a portion of sulfur dioxide and nitrogen dioxide from the flue gas in the cooling chamber.

[0092] In the 27th embodiment according to any of the above-described embodiments, the gas conditioning system further comprises an adsorption unit fluidly positioned upstream of the rotary bed assembly and between the exhaust port and the rotary bed assembly, the adsorption unit having a fluid inlet fluidly connected to the exhaust port, and the adsorption unit being configured to receive flue gas from the exhaust port and remove at least a portion of nitrogen oxides from the flue gas.

[0093] In a 28th aspect according to the 27th aspect, the adsorption unit comprises at least one adsorption bed, and the gas conditioning system is configured to guide flue gas from a fluid inlet through at least one adsorption bed, the adsorption bed being configured to reduce the nitrogen oxide content from the flue gas to less than 50 ppm.

[0094] In the 29th aspect according to the 28th aspect, the adsorption bed is configured to reduce the nitrogen oxide content from the flue gas to less than 10 ppm.

[0095] In a 30th embodiment, a method for regulating flue gas includes guiding flue gas from an exhaust port to a rotating packed bed assembly, the rotating packed bed assembly comprising a first rotating packed bed and a second rotating packed bed, guiding the flue gas, absorbing at least a portion of carbon dioxide from the flue gas using an absorbent in the first rotating packed bed, guiding the absorbent together with the absorbed carbon dioxide from the first rotating packed bed to the second rotating packed bed, and desorbing carbon dioxide from the absorbent in the second rotating packed bed.

[0096] In a 31st aspect according to the 30th aspect, the method further includes introducing the desorbed carbon dioxide into a storage system, compressing the carbon dioxide in a compressor of the storage system, and storing the compressed carbon dioxide in a storage tank of the storage system.

[0097] In the 32nd aspect according to the 30th or 31st aspect, the method further includes introducing flue gas from a first rotating packed bed to a water washing station and washing the flue gas with water in a washing chamber of the water washing station.

[0098] In a 33rd embodiment, which is one of the 30th to 32nd embodiments, the rotary packed bed assembly further comprises a third rotary packed bed in series with the first rotary packed bed and including a second portion of an absorbent, the method further includes introducing flue gas from the first rotary packed bed to the third rotary packed bed and absorbing a second portion of carbon dioxide from the flue gas using the second portion of the absorbent in the third rotary packed bed.

[0099] In a 34th aspect according to the 33rd aspect, the method further includes guiding a second portion of the absorbent from a third rotating packed bed to an intercooler fluid-coupled to a first rotating packed bed and a third rotating packed bed, cooling the second portion of the absorbent in the intercooler, and guiding the cooled second portion of the absorbent to the first rotating packed bed.

[0100] In the 35th aspect according to the 33rd aspect, the method further includes guiding a first portion of the absorbent from a first rotating packed bed to an intercooler fluid-coupled to the first and third rotating packed beds, cooling the first portion of the absorbent in the intercooler, and guiding the cooled first portion of the absorbent to the third rotating packed bed.

[0101] In the 36th aspect described in any one of the 30th to 35th aspects, the rotary packed bed assembly further comprises a fourth rotary packed bed in series with a second rotary packed bed, and the method further includes introducing an absorbent from the second rotary packed bed to the fourth rotary packed bed and desorbing at least a portion of carbon dioxide from the absorbent in the fourth rotary packed bed.

[0102] In the 37th aspect according to the 36th aspect, introducing the absorbent from the second rotating packed bed to the fourth rotating packed bed includes introducing the absorbent from the second rotating packed bed to an interheater fluidly coupled to the second and fourth rotating packed beds, heating the absorbent in the interheater, and introducing the heated absorbent to the fourth rotating packed bed.

[0103] In a 38th aspect, which is one of the 30th to 37th aspects, the method further includes receiving flue gas from the exhaust port at a temperature of 150°C to 550°C in a chamber of an oxidation apparatus fluidly positioned between the exhaust port and a rotating packed bed assembly, and converting a portion of the nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide at a temperature of 150°C to 550°C using a reactant within the chamber of the oxidation apparatus.

[0104] In a 39th aspect, which is one of the 30th to 37th aspects, the method further includes receiving flue gas from the exhaust port at a temperature of 150°C to 350°C in a chamber of an oxidation apparatus fluidly positioned between the exhaust port and a rotating packed bed assembly, and converting a portion of the nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide at a temperature of 150°C to 350°C using a reactant within the chamber of the oxidation apparatus.

[0105] In a fortyth aspect, which is one of the thirtyth to thirty-seventh aspects, the method further includes receiving flue gas from the exhaust port at a temperature of 150°C to 310°C in a chamber of an oxidation apparatus fluidly positioned between the exhaust port and a rotating packed bed assembly, and converting a portion of the nitrogen oxides in the flue gas to at least one of nitrogen gas or nitrogen dioxide at a temperature of 150°C to 310°C using a reactant within the chamber of the oxidation apparatus.

[0106] In the 41st aspect, which is one of the 38th to 40th aspects, the reactant includes an oxidizing agent, and the conversion using the reactant in the chamber of the oxidizing apparatus further includes converting a portion of the sulfur oxides in the flue gas to sulfur dioxide using the oxidizing agent.

[0107] In the 42nd embodiment, which is one of the 38th to 41st embodiments, the oxidation apparatus comprises a selective catalytic reduction unit, and the conversion includes converting a portion of the nitrogen oxides in the flue gas into nitrogen gas at a temperature of 150°C to 550°C.

[0108] In a forty-third aspect according to the forty-second aspect, the reactant includes a catalyst, and the conversion of a portion of the nitrogen oxides in the flue gas to nitrogen gas includes guiding the flue gas to come into contact with a mist of the compound solution in the chamber, and further guiding the flue gas and the mist of the compound solution toward the catalyst in the chamber.

[0109] In the 44th aspect according to the 43rd aspect, the compound solution includes a urea solution or an ammonia solution.

[0110] In the 45th aspect described in any one of the 30th to 44th aspects, the method further includes receiving flue gas from the exhaust port in a direct contact cooler fluidly positioned between the exhaust port and the rotating packed bed assembly, and cooling the flue gas to a temperature of 60°C or less by bringing the flue gas into direct contact with seawater within the direct contact cooler.

[0111] In the 46th aspect according to the 45th aspect, cooling includes cooling the flue gas to a temperature of 50°C or less.

[0112] In the 47th aspect according to the 45th or 46th aspect, the method further includes receiving flue gas from a direct contact cooler in an adsorption unit, and removing at least a portion of residual nitrogen oxides from the cooled flue gas in the adsorption unit.

[0113] In a forty-eighth aspect according to the forty-seventh aspect, removing at least a portion of residual nitrogen oxides from cooled flue gas includes guiding cooled flue gas through at least one adsorption bed of an adsorption unit to reduce the nitrogen oxide content of the flue gas to less than 50 ppm.

[0114] In the 49th aspect according to the 48th aspect, removing at least a portion of residual nitrogen oxides from cooled flue gas includes guiding cooled flue gas through at least one adsorption bed of an adsorption unit to reduce the nitrogen oxide content of the flue gas to less than 10 ppm.

[0115] In the 50th embodiment, the vessel is equipped with a gas adjustment system according to any of the preceding embodiments.

[0116] Therefore, this specification and the drawings should be considered illustrative rather than restrictive. Furthermore, the foregoing use of embodiments and other exemplary language does not necessarily refer to the same embodiment or example, but may refer to different embodiments and distinct embodiments, as well as potentially the same embodiment. The above specification has been described in detail with reference to specific exemplary embodiments. However, it will be apparent that various modifications and changes can be made without departing from the broader spirit and scope of this disclosure as set forth in the claims.

Claims

1. A gas conditioning system for removing pollutants, including carbon dioxide, from flue gas, A rotary filling bed assembly fluidly connected to the exhaust port of an engine, wherein the rotary filling bed assembly is configured to receive flue gas from the exhaust port, and the rotary filling bed assembly is A first rotating packed bed containing an absorbent configured to absorb a portion of the carbon dioxide from the flue gas, A second rotating packed bed is configured to receive the absorbent from the first rotating packed bed and to desorb at least a portion of the carbon dioxide from the absorbent, A gas adjustment system comprising a rotating filled bed assembly.

2. The gas adjustment system according to claim 1, wherein the absorbent comprises a liquid solvent.

3. The gas adjustment system according to claim 2, wherein the liquid solvent comprises an amine solvent.

4. The gas conditioning system according to any one of claims 1 to 3, wherein the rotary bed assembly further comprises a water washing station fluidly connected to the first rotary bed, and the water washing station is configured to wash the flue gas from the first rotary bed with water.

5. The gas adjustment system according to claim 4, wherein the water washing station comprises a filling cylinder or a rotating filling bed.

6. The gas conditioning system according to any one of claims 1 to 5, wherein the rotating bed assembly further comprises a third rotating bed in series with the first rotating bed, the third rotating bed containing a second portion of the absorbent, and the third rotating bed configured to absorb the second portion of carbon dioxide from the flue gas.

7. The gas conditioning system according to claim 6, wherein the rotary bed assembly further comprises an intercooler fluidly coupled to the first rotary bed and the third rotary bed, the intercooler being configured to cool the second portion of the absorbent and guide the second portion of the absorbent to the first rotary bed.

8. The gas conditioning system according to claim 6, wherein the rotary packing bed assembly further comprises an intercooler fluidly coupled to the first rotary packing bed and the third rotary packing bed, the intercooler being configured to cool the first portion of the absorbent and guide the first portion of the absorbent to the third rotary packing bed.

9. The gas conditioning system according to any one of claims 1 to 8, wherein the rotating bed assembly further comprises a third rotating bed parallel to the first rotating bed, the first rotating bed being configured to receive a first portion of the flue gas, the third rotating bed being configured to receive a second portion of the flue gas, and the third rotating bed containing a second portion of the absorbent.

10. The gas conditioning system according to any one of claims 1 to 9, wherein the rotary bed assembly further comprises a fourth rotary bed in series with the second rotary bed, the fourth rotary bed being configured to receive the absorbent from the second rotary bed and to desorb at least a portion of the carbon dioxide from the absorbent.

11. The gas conditioning system according to claim 10, wherein the rotary bed assembly further comprises an interheater fluidly coupled to the second rotary bed and the fourth rotary bed, the interheater being configured to heat the absorbent in the second rotary bed and guide the absorbent to the fourth rotary bed.

12. The gas conditioning system according to any one of claims 1 to 11, wherein the rotating bed assembly further comprises a fourth rotating bed parallel to the second rotating bed, the second rotating bed being configured to receive a first portion of the absorbent, and the fourth rotating bed being configured to receive a second portion of the absorbent.

13. The gas adjustment system according to any one of claims 1 to 12, further comprising a storage system fluidly connected to the second rotating packed bed, the storage system being configured to receive the desorbed carbon dioxide, compress the desorbed carbon dioxide with the compressor, and store the carbon dioxide in the storage tank.

14. A gas conditioning system according to any one of claims 1 to 13, further comprising a selective catalytic reduction unit fluidly positioned upstream of the rotary packed bed assembly between the exhaust port and the rotary packed bed assembly, the selective catalytic reduction unit comprising a fluid inlet and a fluid outlet fluidly connected to the exhaust port, and configured to receive the flue gas from the exhaust port through the fluid inlet and convert at least a portion of the nitrogen oxides in the flue gas into nitrogen gas.

15. The gas adjustment system according to claim 14, wherein the selective catalytic reduction unit receives the flue gas exhausted from the engine at a temperature of 150°C to 550°C and converts a portion of the nitrogen oxides in the flue gas into nitrogen gas at a temperature of 150°C to 550°C.

16. The gas adjustment system according to claim 15, wherein the selective catalytic reduction unit receives the flue gas exhausted from the engine at a temperature of 150°C to 350°C and converts a portion of the nitrogen oxides in the flue gas into nitrogen gas at a temperature of 150°C to 350°C.

17. The gas adjustment system according to claim 16, wherein the selective catalytic reduction unit receives the flue gas exhausted from the engine at a temperature of 150°C to 310°C and converts a portion of the nitrogen oxides in the flue gas into nitrogen gas at a temperature of 150°C to 310°C.

18. The gas adjustment system according to any one of claims 14 to 17, wherein the selective catalytic reduction unit comprises a housing defining a chamber and a compound inlet configured to introduce a mist of a compound solution into the chamber, and the fluid inlet is configured to guide the flue gas into contact with the mist of the compound solution in the chamber.

19. The gas adjustment system according to claim 18, wherein the compound solution contains urea or ammonia.

20. The gas conditioning system according to claim 18 or 19, wherein the selective catalytic reduction unit includes a catalyst disposed in the chamber, and the catalyst is configured to come into contact with the flue gas and the mist of the compound solution in the chamber.

21. An oxidation apparatus comprising a fluid inlet fluidly connected to the flue gas exhausted from the engine and a fluid outlet fluidly connected to the rotating bed assembly, wherein the oxidation apparatus is configured to receive the flue gas exhausted from the engine through the fluid inlet and to convert at least a portion of the nitrogen oxides in the flue gas to nitrogen dioxide and at least a portion of the sulfur oxides in the flue gas to sulfur dioxide. A gas adjustment system according to any one of claims 1 to 13, further comprising:

22. A direct contact cooler positioned upstream of the rotary packed bed assembly and fluidly positioned between the exhaust port and the rotary packed bed assembly, wherein the direct contact cooler comprises a fluid inlet fluidly connected to the exhaust port, a housing surrounding a cooling chamber, and a fluid outlet, and the direct contact cooler is configured to guide the flue gas into contact with seawater present in the cooling chamber and to cool the flue gas to a temperature of 60°C or less. A gas adjustment system according to any one of claims 1 to 21, further comprising:

23. The gas conditioning system according to claim 22, wherein the direct contact cooler is configured to guide the flue gas into contact with seawater present in the cooling chamber, thereby cooling the flue gas to a temperature of 50°C or less.

24. The direct contact cooler, The housing surrounding the cooling chamber, A rotor drum, which is disposed within the housing and is rotatable around a rotation axis, A seawater inlet is fluid-connected to the rotor drum, A seawater outlet is fluid-connected to the housing, The fluid inlet connected to the housing, The third rotating filling bed comprises a fluid outlet fluidly connected to the rotor drum, The flue gas is guided from the fluid inlet to the fluid outlet, and the seawater is guided from the seawater inlet to the seawater outlet. The gas adjustment system according to claim 22 or claim 23.

25. The gas adjustment system according to claim 24, wherein the flue gas is arranged in a counterflow with the seawater in the rotor drum when the third rotating bed is in use.

26. The gas conditioning system according to any one of claims 22 to 25, wherein the direct contact cooler is provided with a seawater inlet for introducing the seawater into the cooling chamber, and the seawater is configured to remove at least a portion of sulfur dioxide and nitrogen dioxide from the flue gas in the cooling chamber.

27. An adsorption unit is fluidly positioned upstream of the rotary packed bed assembly and between the exhaust port and the rotary packed bed assembly, wherein the adsorption unit includes a fluid inlet fluidly connected to the exhaust port, and is configured to receive the flue gas from the exhaust port and remove at least a portion of the nitrogen oxides from the flue gas. A gas adjustment system according to any one of claims 1 to 26.

28. The gas conditioning system according to claim 27, wherein the adsorption unit comprises at least one adsorption bed, the gas conditioning system is configured to guide the flue gas from the fluid inlet through the at least one adsorption bed, and the adsorption bed is configured to reduce the nitrogen oxide content from the flue gas to less than 50 ppm.

29. The gas adjustment system according to claim 28, wherein the adsorption bed is configured to reduce the nitrogen oxide content from the flue gas to less than 10 ppm.

30. A method for adjusting flue gas, The means of guiding the flue gas from the exhaust port to a rotary filling bed assembly, wherein the rotary filling bed assembly comprises a first rotary filling bed and a second rotary filling bed. In the first rotating packed bed, an absorbent is used to absorb at least a portion of the carbon dioxide from the flue gas, The absorbent, along with the absorbed carbon dioxide, is guided from the first rotating packed bed to the second rotating packed bed. Desorbing the carbon dioxide from the absorbent in the second rotating packed bed, A method that includes this.

31. The desorbed carbon dioxide is guided into the storage system, Compressing the carbon dioxide with the compressor of the storage system, The storage system includes storing the compressed carbon dioxide in its storage tank, The method according to claim 30, further comprising:

32. The flue gas is guided from the first rotating filling bed to the water washing station, The flue gas is washed with water in the washing chamber of the water washing station, The method according to claim 30 or claim 31, further comprising:

33. The rotary filling bed assembly further comprises a third rotary filling bed in series with the first rotary filling bed, which includes a second portion of the absorbent, and the method The flue gas is guided from the first rotating filling bed to the third rotating filling bed, The second portion of the absorbent is used within the third rotating packed bed to absorb the second portion of carbon dioxide from the flue gas, The method according to any one of claims 30 to 32, further comprising:

34. The second portion of the absorbent is guided from the third rotating bed to an intercooler fluidly coupled to the first rotating bed and the third rotating bed, Cooling the second portion of the absorbent using the intercooler, and guiding the cooled second portion of the absorbent to the first rotating bed, The method according to claim 33, further comprising:

35. The first portion of the absorbent is guided from the first rotating packed bed to an intercooler fluidly coupled to the first rotating packed bed and the third rotating packed bed, The first portion of the absorbent is cooled using the intercooler, To guide the first portion of the cooled absorbent to the third rotating bed, The method according to claim 33, further comprising:

36. The rotary filling bed assembly further comprises a fourth rotary filling bed in series with the second rotary filling bed, and the method is The absorbent is guided from the second rotating bed to the fourth rotating bed, In the fourth rotating packed bed, at least a portion of the carbon dioxide is desorbed from the absorbent, The method according to any one of claims 30 to 35, further comprising:

37. Guiding the absorbent from the second rotating bed to the fourth rotating bed is The absorbent is guided from the second rotating packed bed to an interheater fluidly coupled to the second rotating packed bed and the fourth rotating packed bed, Heating the absorbent using the interheater, The heated absorbent is guided to the fourth rotating bed, The method according to claim 36, including the method described in claim 36.

38. In the chamber of the oxidation apparatus, which is fluidly positioned between the exhaust port and the rotating packed bed assembly, the flue gas is received from the exhaust port at a temperature of 150°C to 550°C. Using a reactant in the chamber of the oxidation apparatus, a portion of the nitrogen oxides in the flue gas is converted into at least one of nitrogen gas or nitrogen dioxide at a temperature of 150°C to 550°C. The method according to any one of claims 30 to 37, further comprising:

39. In the chamber of the oxidation apparatus, which is fluidly positioned between the exhaust port and the rotating packed bed assembly, the flue gas is received from the exhaust port at a temperature of 150°C to 350°C. Using a reactant in the chamber of the oxidation apparatus, a portion of the nitrogen oxides in the flue gas is converted into at least one of nitrogen gas or nitrogen dioxide at a temperature of 150°C to 350°C. The method according to any one of claims 30 to 37, further comprising:

40. In the chamber of the oxidation apparatus, which is fluidly positioned between the exhaust port and the rotating packed bed assembly, the flue gas is received from the exhaust port at a temperature of 150°C to 310°C. Using a reactant in the chamber of the oxidation apparatus, a portion of the nitrogen oxides in the flue gas is converted into at least one of nitrogen gas or nitrogen dioxide at a temperature of 150°C to 310°C. The method according to any one of claims 30 to 37, further comprising:

41. The reactant includes an oxidizing agent, The conversion using the reactant in the chamber of the oxidation apparatus is to convert a portion of the sulfur oxides in the flue gas into sulfur dioxide using the oxidizing agent. The method according to any one of claims 38 to 40, further comprising:

42. The method according to any one of claims 38 to 41, wherein the oxidation apparatus comprises a selective catalytic reduction unit, and the conversion includes converting a portion of the nitrogen oxides in the flue gas into nitrogen gas at a temperature of 150°C to 550°C.

43. The method according to claim 42, wherein the reactant includes a catalyst, and the conversion of a portion of the nitrogen oxides in the flue gas into nitrogen gas is guided to bring the flue gas into contact with a mist of the compound solution in the chamber, and the flue gas and the mist of the compound solution are further guided toward the catalyst in the chamber.

44. The method according to claim 43, wherein the compound solution comprises a urea solution or an ammonia solution.

45. A direct contact cooler is fluidly positioned between the exhaust port and the rotating packed bed assembly, which receives the flue gas from the exhaust port, The flue gas is brought into direct contact with seawater within the direct contact cooler to cool the flue gas to a temperature of 60°C or lower. The method according to any one of claims 30 to 44, further comprising:

46. The method according to claim 45, wherein the cooling includes cooling the flue gas to a temperature of 50°C or lower.

47. The adsorption unit receives the flue gas from the direct contact cooler, The adsorption unit removes at least a portion of the residual nitrogen oxides from the cooled flue gas, The method according to claim 45 or claim 46, further comprising:

48. The method according to claim 47, wherein removing at least a portion of residual nitrogen oxides from the cooled flue gas includes guiding the cooled flue gas through at least one adsorption bed of the adsorption unit to reduce the nitrogen oxide content of the flue gas to less than 50 ppm.

49. The method according to claim 48, wherein removing at least a portion of residual nitrogen oxides from the cooled flue gas includes guiding the cooled flue gas through at least one adsorption bed of the adsorption unit to reduce the nitrogen oxide content of the flue gas to less than 10 ppm.

50. A vessel comprising a gas adjustment system according to any one of claims 1 to 49.

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